EPA-450/3-81-009a
     Metallic Mineral
   Processing Plants —
Background Information
for Proposed Standards

 Volume 1: Chapters 1 -9
    Emission Standards and Engineering Division
    U.S. ENVIRONMENTAL PROTECTION AGENCY
       Office of Air, Noise, and Radiation
    Office of Air Quality Planning and Standards
    Research Triangle Park, North Carolina 27711


             August 1982

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This report has been reviewed by the Emission Standards and
Engineering Division of the Office of Air Quality Planning
and Standards, EPA, and approved for publication.  Mention
of trade names or commercial products is not intended to
constitute endorsement or recommendation for use.  Copies
of this report are available through the Library Services
Office (MD-35), U. S. Environmental Protection Agency,
Research Triangle Park, N. C. 27711, or from National;
Technical Information Service, 5285 Port Royal Road,'
Springfield, Virginia  22161.                      -
            PUBLICATION NO. EPA-450/3-81-009a
                              n

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                       ENVIRONMENTAL PROTECTION AGENCY

                           Background Information
                                  and Draft
                       Environmental Impact Statement
                            for Metallic Mineral
                              Processing Plants
                                Prepared by:
Don R. Goodwin
Director, Emission Standards and Engineering Division
U. S. Environmental Protection Agency
Research Triangle Park, NC  27711
                             (Date)
1.   The proposed standards of performance would limit emissions of
     particulate matter from new, modified, and reconstructed metallic
     mineral processing plants.  Section 111 of the Clean Air Act
     (42 U.S.C 7411), as amended, directs the Administrator to establish
     standards of performance for any category of new stationary source
     of air pollution that ". . . causes or contributes significantly to
     air pollution which may reasonably be anticipated to endanger
     public health or welfare."

2.   Copies of this document have been sent to the following Federal
     Departments:  Labor, Health and Human Services, Defense, Transportation,
     Agriculture, Commerce, Interior, and Energy, as well as the National
     Science Foundation, the Council on Environmental  Quality, State and
     Territorial Air Pollution Program Administrators, the Association
     of Local Air Pollution Control Officials, EPA Regional Administrators,
     and other interested parties.

3.   The comment period for review of this document is 60 days.
     Mr. Gene Smith may be contacted regarding the date of the comment
     period.

4.   For additional information contact:

     Mr. Gene Smith
     Standards Development Branch (MD-13)
     U.S. Environmental Protection Agency
     Research Triangle Park, NC  27711
     telephone:  (919) 541-5624

5.   Copies of this document may be obtained from:
     U. S. EPA Library (MD-35)
     Research Triangle Park, NC
27711
     National Technical Information Service
     5285 Port Royal Road
     Springfield, VA  22161

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                           TABLE OF CONTENTS
Section                                                               Page
1.0  Summary	.1-1
     1.1  Regulatory Alternatives	1-2
     1.2  Environmental Impact and Energy Impact .  .  	   1-4
     1.3  Economic Impact.	1-7
2.0  Introduction.	.  .  .	2-1
     2.1  Background and Authority for Standards .	2-1
     2.2  Selection of Categories of Stationary Sources.  ......   2-5
     2.3  Procedure for Development of Standards of Performance.  .  .   2-6
     2.4  Consideration of Costs	2-8
     2.5  Consideration of Environmental  Impacts 	   2-9
     2.6  Impact on Existing Sources	2-11
     2.7  Revision of Standards of Performance 	   2-11
3.0  The Metallic Mineral Processing Industry	3-1
     3.1  Introduction . . .	3-1
     3.2  Metallic Mineral Processes of Facilities  and  Their
          Emissions	3-5
          3.2.1  Crushing Operations 	   3-12
          3.2.2  Emissions from Crushing  Operations	  .   3-25
          3.2.3  Screening Operations	3-29
          3.2.4  Emissions from Screening Operations  	   3-33
          3.2.5  Grinding Operations	3-33

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Section                                                               Page
          3.2.6  Emissions from Grinding Operations	   3-37
          3,2.7  Conveying Operations	   3-37
          3.2.8  Emissions from Conveying Operations	 ,,  .  .   3-44
          3.2.9  Drying Operations 	   3-44
          3.2.10 Emissions from Drying Operations	   3-48
          3.2.11 Bagging and Bulk Loading Operations 	   3-48
          3.2.12 Emissions from Bagging and Bulk Loading
                 Operations	   3-48
          3.2.13 Emission Factors for Related Industries 	   3-49
     3.3  Process Emissions Allowed Under Current State
          Regulations	   3-49
     3.4  References for Chapter 3	   3-55
4.0  Emission Control Techniques 	   4-1
     4.1  Introduction	   4-1
     4.2  Fabric Filters 	  .....   4-5
     4.3  Performance Data for Fabric Filter Baghouses .......   4-9
          4.3.1  Particulate Emission Data	  . „  .  .   4-9
          4.3.2  Visible Emission Data 	  .....   4-27
     4.4  Scrubbers	4-31
     4.5  Performance Data for Wet Scrubbers	   4-35
          4.5.1  Particulate Emission Data 	  .....   4-35
          4.5.2  Visible Emissions Data:  Wet Scrubbers	4-52
     4.6  Mathematical  Modelling of Venturi-Scrubber Efficiency.  .  .   4-52
     4.7  Exhaust Systems and Ducting	   4-59
          4.7.1  Conveyor Belt Dust Control	   4-59
          4.7.2  Crushers and Dry Grinders . .	   4-62
                                   VI

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Section                                                               Page
          4.7.3  Screens	4-64
          4.7.4  Raw Materials and Product Storage in Bins 	   4-67
          4.7.5  Product Handling	4-67
          4.7.6  Drying of Product	4-70
     4.8  Performance Data for Exhaust Systems	4-72
     4.9  Electrostatic Preci pita tors	4-72
     4.10 Conclusions from Test and Modelling Data .... 	   4-78
     4.11 References for Chapter 4	4-86
5.0  Modifications and Reconstructions 	   5-1
     5.1  Modification	5-1
     5.2  Reconstruction	5-2
6.0  Model Plants and Regulatory Options 	   6-1
     6.1  Introduction	   6-1
     6.2  Model Plants	6-1
          6.2.1  Inclusive Model Facility	   6-2
          6.2.2  Process Units	6-2
     6.3  Regulatory Alternatives.	   6-9
          6.3.1  Regulatory Alternative 1	   6-10
          6.3.2  Regulatory Alternative 2	6-10
          6.3.3  Regulatory Alternative 3	6-11
          6.3.4  The "Worst-Case Analysis Method"	6-11
          6.3.5  Control Equipment Options for Each Regulatory
                 Alternative . .	   6-12
     6.4  Model Plant Parameters	   6-12
          6.4.1  Introduction	6-12
          6.4.2  Aluminum Ore Processing Facility. .........   6-15
                                    VII

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Section                                                               Page
          6.4.3  Copper Ore Processing Facility	6-23
          6.4.4  Gold Ore Processing Facility	6-29
          6.4.5  Iron Ore Processing Facility	6-36
          6.4.6  Lead/Zinc Ore Processing Facility 	   6-42
          6.4.7  Molybdenum Ore Processing Facility	6-48
          6.4.8  Silver Ore Processing Facility	6-54
          6.4.9  Titanium/Zirconium Sand Type Ore Processing
                 Facility.	6-60
          6.4.10 Tungsten Ore Processing Facility	6-65
          6.9.11 Uranium Ore Processing Facility 	   6-71
     6.5  References for Chapter 6	6-76
7.0  Environmental Impact.	7-1
     7.1  Air Pollution Impact	7-1
          7.1.1  National Particulate Emissions	7-1
          7.1.2  Dispersion Analysis 	   7-3
     7.2  Water Pollution Impact 	   7-5
     7.3  Solid Waste Disposal Impact	7-14
     7.4  Energy Impact	7-15
     7.5  Noise Impact	7-16
     7.6  Other Environmental Concerns 	   7-16
          7.6.1  Irreversible and Irretrievable Commitment of
                 Natural  Resources 	   7-16
          7.6.2  Environmental Impact of Delayed Standards 	   7-16
     7.7  References for Chapter 7	7-18
8.0  Costs	   8-1
                                   vm

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Section
Paqe
     8.1  Costs of Air Pollution Control for Metallic Mineral
          Processing Industries	  8-1
          8.1.1  Summary of Cost Results	8-1
          8.1.2  Product Recovery Credits and Dust Disposal Costs.  .  8-2
          8.1.3  Costs of Control Options:  Scrubbers and
                 Baghouses	8-3
          8.1.4  Capital Costs for Metallic Mineral Processing
                 Units	8-4
     8.2  Other Cost Considerations	8-44
          8.2.1  Other Air Pollution Control Costs 	  8-44
          8.2.2  Control Costs Resulting from OSHA Regulations  .  .  .  8-47
          8.2.3  Water Pollution Control Requirements	8-48
     8.3  References for Chapter 8 . .  .	•  •	8~74
 9.0  Economic  Impact	9-1
     9.1  Industry  Characterization	9-1
          9.1.1  Aluminum	9-3
          9.1.2  Copper	9-12
          9.1.3  Gold	9-22
          9.1.4  Iron Ore	9-31
          9.1.5  Lead	9-42
          9.1.6  Molybdenum.	  9-53
          9.1.7  Silver	9-60
          9.1.8  Titanium.	  9-67
          9.1.9  Tungsten.	•  •  •  9-74
          9.1.10 Uranium	.'	9-81
          9.1.11 Zinc.	9-89
                                   ix

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Section
Paqe
          9.1.12 Zirconium 	   9-94
          9.1.13 Strategic Stockpile	9-94
          9.1.14 References Section 9.1	   9-101
     9.2  Economic Impact Assessment 	   9-103
          9.2.1  Introduction and Summary	9-103
          9.2.2  Methodology	   9-105
          9.2.3  Findings	9-108
          9.2.4  Aluminum	9-108
          9.2.5  Copper	   9-110
          9.2.6  Gold	9-113
          9.2.7  Iron Ore	9-114
          9.2.8  Lead/Zinc	9-116
          9.2.9  Molybdenum	9-118
          9.2.10 Silver	   9-120
          9.2.11 Titanium/Zirconium	   9-121
          9.2.12 Tungsten	9-122
          9.2.13 Uranium 	   9-123
     9.3  Socio-Economic Impact Assessment 	 ...   9-125
     9.4  References for Section 9.2 and 9.3	9-128

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                            LIST OF TABLES
Table
 No.                                                                  Page
 1-1   Assessment of Environmental, Energy, and Economic Impacts'
       for Each Regulatory Alternative Considered for New
       Metallic Mineral Processing Plants. .  	  1-5
 3-1   Metal Ore Constituents	.3-3
 3-2   Metals Not Included^™ This Document.  ..'..-	.  .  3-6
 3-3   U.S. Metallic Mineral Ores and Their Process Products ....  3-7
 3-4   Major Uses of Metals	3-8
 3-5   Typical Ore Processing Operations by Metal Ore Processing
       Industry	  3-10
 3-6   Operating Data for Jaw Crushers	3-15
 3-7   Operating Data for Gyratory Crushers	3-18
 3-8   Operating Data for Impact Crushers	3-23
 3-9   Factors Affecting Emissions from Crushing Operations	3-28
 3-10  Power Requirements for Vibrating Screens	  3-34
 3-11  Parameters for Screening Operations 	  ....  3-36
 3-12  Power Requirements for Vibrating Feeders	3-40
 3-13  Operating Parameters for Belt Conveyors	 .  .  3-42
 3-14  Particulate Emission Factors for Rock-Handling Processes. .  .  3-50
 3-15  State Process Weight Equations	3-51
 3-16  Metallic Mineral Process Weight Curves	  3-53

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Table
No.
3-17

4-1
4-2
4-3
4-4

4-5

4-6

4-7
4-8

4-9


6-1

6-2

6-3

6-4
6-5

6-6

6-7
6-8




Baseline Emissions Based on Modelling of Wet Scrubber
Performance 	 	
Baghouse Units Tested By EPA 	
Opacity Measurements From Baghouse Exhaust Stacks 	
Opacity Measurements From Wet Scrubber Exhaust Stacks ....
Emission Concentrations Possible With Venturi Scrubbers
Given Worst- and Moist-Case Conditions 	
Modelling of Venturi Scrubber Performance With Dryer
Exhaust Characteristics 	
Exhaust Requirements for Metallic Mineral Processing
Operations 	
Recommended Minimum Duct Velocities 	 	
Summary of Visible Emissions Measurements at Duct Inlets
(Pickup Points) at Metallic and Nonmetallic Facilities. . . .
Average Uncontrolled Emissions Levels From All Processes
Tested by EPA in the Metallic and Nonmetallic Mineral
Processing Industries ....... 	
List of Process Equipment and Air Volume Used in Determining
Model Plants 	 	
List of Process Equipment and Air Volume Requirements Used
In Determining Model Aluminum Ore Plants 	
Stack and Control System Parameters for Aluminum Ore Model
Plants 	
Energy Requirements for an Aluminum Ore Processing Plant. . .
List of Process Equipment and Air Volume Requirements Used
In Determining Model Copper Ore Plants 	
Stack and Control System Parameters for Copper Ore Model
Plants 	 	 • • •
Energy Requirements for a Copper Ore Processing Plant . . . .
List of Process Equipment and Air Volume Requirements Used
in Determining Model Gold Ore Processing Plants 	
.xii

Page

3-54
4-10
4-30
4-53

4-57

4-58
4f f\
-60
4-61

4-73


4-79

6-4

6-17

6-19
6-21

6-24

6-26
6-28

6-30
^M

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Table
 No.

 6-9
 6-10

 6-11


 6-12


 6-13

 6-14


 6-15


 6-16

 6-17


 6-18


 6-19

 6-20


 6-21

 6-22

 6-23



 6-24


 6-25


 6-26
Stack and Control System Parameters for Gold Ore Model
Plants	
Energy Requirements for a Gold Ore Processing Plant
List of Process Equipment and Air Volume Requirements Used
in Determining Model Iron Ore Processing Plants ......
Stack and Control System Parameters for Iron Ore Model
Plants	
Energy Requirements for an Iron Ore Processing Plant.
List of Process Equipment and Air Volume Requirements Used
in Determining Model Lead/Zinc Ore Processing Plants. .  .  .

Stack and Control System Parameters for Lead/Zinc Ore Model
Plant ........... 	 . 	

Energy Requirements for a Lead/Zinc Ore Processing Plant.  .

List of Process Equipment and Air Volume Requirements Used
in Determining Model Molybdenum Ore Processing Plants .  .  .

Stack and Control System Parameters for Molybdenum Ore Model
Plants	

Energy Requirements for Molybdenum Ore Processing Plant .  .

List of Process Equipment arid Air Volume Requirements Used
in Determining Model Silver Ore Processing Plants 	
Stack and Control System Parameters for Silver Ore Plants .

Energy Requirements for Silver Ore Processing Plants. .  . .
List of Process Equipment and Air Volume Requirements Used
in Determining Model Titanium/Zirconium Sand Type Ore
Processing Plants  	  	
Stack and Control System Parameters for Titanium/Zirconium
Sand Type Ore Model Plant	
List of  Process  Equipment and Air Volume Requirements Used
in  Determining Model Tungsten Ore Processing Plants  . .  .  .

Stack  and  Control  System Parameters  for Tungsten Ore Model
Plants	
                                                               Page
6-32

6-34


6-37


6-39

6-41


6-43


6-45

6-47


6-49


6-51'

6-53


6-55

6-57

6-59



6-61


6-63


6-66


6-68

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Table
 No.
Page

6-70
 6-27  Energy Requirements for Tungsten Ore Processing Plant ...

 6-28  List of Process Equipment and Air Volume Requirements Used
       in Determining Model Uranium Ore Processing Plants	6-72

 6-29  Stack and Control System Parameters for Uranium Ore Model
       Plants	6-74

 7-1   New Capacity and Operating Parameters for Model Plants Used
       for Estimating Environmental Impacts. ... 	  7-2

 7-2   Air Impacts of the Regulatory Alternatives for the Metallic
       Mineral Processing Model Plants 	  . 	  7-4

 7-3   Particulate Matter Concentrations (Annual Averages) in the
       Vicinity of Metallic Mineral Plants Operating Under
       Regulatory Alternative 1	7-6

 7-4   Particulate Matter Concentrations (Annual Averages) in the
       Vicinity of Metallic Mineral Plants Operating Under
       Regulatory Alternative 2	-	•  7-7

 7-5   Particulate Matter Concentrations (Annual Averages) in the
       Vicinity of Metallic Mineral Plants Operating Under
       Regulatory Alternative 3	7-8

 7-6   Particulate Matter Concentrations (24-Hour Averages) in  the
       Vicinity of Metallic Mineral Plants Operating Under
       Regulatory Alternative 1	7-9

 7-7   Particulate Matter Concentrations (24-Hour Averages) in  the
       Vicinity of Metallic Mineral Plants Operating Under-
       Regulatory Alternative 2	7-10

 7-8   Particulate Matter Concentrations (24-Hour Averages) in  the
       Vicinity of Metallic Mineral Plants Operating Under-
       Regulatory Alternative 3	7-11

 7-9   Water Impacts of the Control Options Under  the Three
       Regulatory Alternatives  for  the Metallic Mineral  Processing
       Model Plants	  7-13

 7-10  Energy  Impacts of the Control Options Using the Three
       Regulatory Alternatives  for  the Metallic Mineral  Processing
       Model Plants	7-17
                                    xiv

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Table
 No.
Pac
 8-1   Costs of Regulatory Alternatives for the 140 Mg (150 ton)/
       Hour Aluminum Ore Processing Industry Model Plant (1979
       Dollars)	 .	8-6

 8-2   Costs of Regulatory Alternatives for the 270 Mg (300 Ton)/
       Hour Aluminum Ore Processing Industry Model Plant (1979
       Dollars)	•  .  8-7

 8-3   Costs of Regulatory Alternatives for the 140 Mg (150 ton)/
       Hour Copper Ore Processing Industry Model Plant (1979
       Dollars)	8-8

 8-4   Costs of Regulatory Alternatives for the 540 Mg (600 Ton)/
       Hour Copper Ore Processing Industry Model Plant (1979
       Dollars)	8-9

 8-5   Costs of Regulatory Alternatives for the 68 Mg (75 Ton)/
       Hour Gold Ore Processing Industry Model Plant (1979
       Dollars)	8-10

 8-6   Costs of Regulatory Alternatives for the 140 Mg (150 Ton)/
       Hour Gold Ore Processing Industry Model Plant (1979
       Dollars)	  .  8-11

 8-7   Costs of Regulatory Alternatives for the 1,100 Mg (1,200 Ton)/
       Hour Iron Ore Processing Industry Model Plant (1979
       Dollars)	8-12

 8-8   Costs of Regulatory Alternatives for the 2,200 Mg (2,400 Ton)/
       Hour Iron Ore Processing Industry Model Plant (1979
       Dollars).	  8-13

 8-9   Costs of Regulatory Alternatives for the 270 Mg (300 Ton)/
       Hour Lead/Zinc Ore Processing  Industry Model Plant  (1979
       Dollars)	8-14

 8-10  Costs of Regulatory Alternatives for the 540 Mg (600 Ton)/
       Hour Lead/Zinc Ore Processing  Industry Model Plant  (1979
       Dollars)	  .  8-15

 8-11  Costs of Regulatory Alternatives for the 270 Mg (300 Ton)/
       Hour Molybdenum Ore Processing Industry Model Plant (1979
       Dollars)	8-16

 8-12  Costs of Regulatory Alternatives for the 1100 Mg  (1200 Ton)/
       Hour Molybdenum Ore Processing Industry Model Plant (1979
       Dollars).	8-17
                                    xv

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Table
 No.
Page
 8-13  Costs of Regulatory Alternatives for the 45 Mg (50 Ton)/
       Hour Silver Ore Processing Industry Model Plant (1979
       Dollars)	8-18

 8-14  Costs of Regulatory Alternatives for the 140 Mg (150 Ton)/
       Hour Silver Ore Processing Industry Model Plant (1979
       Dollars)	  8-19

 8-15  Costs of Regulatory Alternatives for the 270 Mg (300 Ton)/
       Hour Titanium/Zirconium Sand Type Ore Processing Industry
       Model Plant	8-20

 8-16  Costs of Regulatory Alternatives for the 540 Mg (600 Ton)/
       Hour Titanium/Zirconium Sand Type Ore Processing Industry
       Model Plant (1979" Dollars)	  .  8-21

 8-17  Costs of Regulatory Alternatives for the 23 Mg (25 Ton)/
       Hour Tungsten Ore Processing Industry Model Plant (1979
       Dollars)	8-22

 8-18  Costs of Regulatory Alternatives for the 23 Mg (25 Ton)/
       Hour Uranium Ore Processing Industry Model Plant (1979
       Dollars)	8-23

 8-19  Costs of Regulatory Alternatives for the 68 Mg (75 Ton)/
       Hour Uranium Ore Processing Industry Model Plant (1979
       Dollars)	8-24

 8-20  Marginal Cost Effectiveness of Regulatory Alternatives for
       the Aluminum Ore Processing Industry Model Plants (1979
       Dollars)	8-25

 8-21  Marginal Cost Effectiveness of Regulatory Alternatives for
       the Copper Ore Processing Industry Model Plants (1979
       Dollars)	8-26

 8-22  Marginal Cost Effectiveness of Regulatory Alternatives for
       the Gold Ore Processing Industry Model Plants  (1979
       Dollars)	8-27

 8-23  Marginal Cost Effectiveness of Regulatory Alternatives for
       the Iron Ore Processing Industry Model Plants  (1979
       Dollars).	  .  8-28

 8-24  Marginal Cost Effectiveness of Regulatory Alternatives for
       the Lead/Zinc Ore Processing Industry Model Plants  (1979
       Dollars)	,.  .  8-29
                                    xvi

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Table
 No.

 8-25
 8-26



 8-27



 8-28



 8-29



 8-30

 8-31


 8-32


 8-33


 8-34


 8-35


 8-36


 8-37

 8-38

 8-39

 8-40
Marginal Cost Effectiveness of Regulatory Alternatives for
the Molybdenum Ore Processing Industry Model Plants (1979
Dollars)	

Marginal Cost Effectiveness of Regulatory Alternatives for
the Silver Ore Processing Industry Model Plants (1979
Dollars)	

Marginal Cost Effectiveness of Regulatory Alternatives for
the Titanium/Zirconium Ore Processing Industry Model Plants
(1979 Dollars)	

Marginal Cost Effectiveness of Regulatory Alternatives for
the Tungsten Ore Processing Industry Model Plants (1979
Dollars)	. . .  .

Marginal Cost Effectiveness of Regulatory Alternatives for
the Uranium Ore Processing Industry Model Plants (1979
Dollars)	

Parameters for Product Recovery Credits  (1979 Dollars). . .  .

Specifications for Scrubber and Fabric Filter Control
Options 	

Direct Capital Cost Factors for a Wet Scrubber as a Function
of Equipment Cost	

Indirect Capital Cost Factors for a Wet  Scrubber as a
Function of Equipment Cost	
Direct Capital Cost Factors for a Baghouse as a Function
of Equipment Cost  ..... 	
 Indirect Capital Cost Factors for a Baghouse as a Function
 of Equipment Cost  .  . .	
Bases for Scrubber and Fa-trie Filter Annualized Costs
(1979 Dollars)	  .
 Fixed-Capital  Investment	

 Total Capital  Requirements for a 25 TPH Tungsten Plant.  .  .

 Control Costs  for Model Cooper Smelting Facilities	

 Control Costs  for Model Zinc Smelters  	
                                                               Paqe
8-30



8-31



8-32



8-33



8-34

8-35


8-36


8-37


8-37


8-38


8-38


8-39

8-40

8-43

8-50

8-52
                                   xvn

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Table
 No.                                                                  Page

 8-41  Control Costs for Model Lead Smelters .	8-54

 8-42  Cost of Potline Controls for Aluminum Reduction Smelters.  .  .   8-56

 8-43  Control Costs for Prebake Anode Baking Furnaces ........   8-57

 8-44  Control Costs of Meeting Performance Standard (0.22 gr/
       dscf) for Typical New Two-Vessel Basic Oxygen Process
       Furnaces	8-58

 8-45  Electric Arc Furnace Control Costs for Shop With Three
       100 Ton Furnaces Using Fabric Filter Control Device .....   8-59

 8-46  Comparison of Capital and Annual Costs for an Open and
       Sealed Furnace	8-60

 8-47  Control Costs of the Lead NAAQS for Model  Primary Lead and
       Primary Copper Smelters 	   8-61

 8-48  Primary Lead Smelting and Refining Costs of Compliance to
       Meet the Occupational Exposure to Lead Regulation	8-62

 8-49  Cost for the Iron Ore Processing Industry for Various Types
       of Waste Treatment Technologies to Meet the BAT Standards .  .   8-63

 8-50  Cost for the Copper Ore Processing Industry for Various
       Types of Water Treatment Technologies to Meet the BAT
       Standards	8-65

 8-51  Costs for the Lead/Zinc Ore Processing Industry for Various
       Types of Water Treatment Technologies to Meet the BAT
       Standards	8-66

 8-52  Costs for the Gold and Silver Ore Processing Industry for
       Various Types of Water Treatment Technologies to Meet the
       BAT Standards	8-67

 8-53  Costs for the Aluminum Ore Processing Industry for Various
       Types of Water Treatment Technologies to Meet the BAT
       Standards	   8-68

 8-54  Costs for the Ferroalloy Ore Processing Industry for Various
       Types of Water Treatment Technologies to Meet the BAT
       Standards	   8-69

 8-55  Costs for the Uranium/Vanadium Ore Processing Industry for
       Various Types of Waste Treatment Technologies to Meet the
       BAT Standards	8-70
                                   XV11T

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 Table
  No.                                                                  Page
  9-1   Metallic Mineral Processing Products	9-2
  9-2   Production  Profile:  Bauxite	9-5
  9-3   Bauxite Industry Characteristics	9-6
  9-4   Aluminum Ore  (Bauxite) Processing Plants  (Refineries)  ....  9-7
  9-5   Product Uses:  Bauxite.  .  .	9-8
  9-6   Production  Profile:  Aluminum  	  9-9
  9-7   Product Uses:  Aluminum  Metal	  9-10
                                                                          t
  9-8   Price  History:  Aluminum	9-11
•  9-9   Production  Profile:  Copper 	  9-14
  9-10  Price  History:  Copper	9-15
  9-11  Product Uses:  Copper	9-16
  9-12  Industry Characteristics:  Copper	  .  .  .  9-16
  9-13  Copper Ore  Processing Plants	9-17
  9-14  Product Uses:  Gold	.9-24
  9-15  Price  History:  Gold.  	  9-25
  9-16  Production  Profile:  Gold	  9-26
  9-17  Industry Characteristics:  Gold	  .  9-27
  9-18  Gold Ore Processing  Plants	  9-28
  9-19  Production  Profile:  Iron  Ore	  .  9-32
  9-20  Industry Characteristics:  Iron	9-33
  9-21  Iron Ore Processing  Plants	9-34
  9-22  Product Uses:  Iron	9-40
  9-23  Price  History:   Iron In  Ore	  .  9-41
  9-24  Production  Profile:  Lead	9-44
                                    xix

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Table
 No.                                                                  Paje.
 9-25  Production Uses:  Lead	9-45
 9-26  Price History:  Lead	   9-46
 9-27  Industry Characteristics:  Lead 	   9-47
 9-28  Lead And/Or Zinc Processing Plants	9-48
 9-29  Production Profile:  Molybdenum	  .  .   9-55
 9-30  Product Uses:  Molybdenum 	   9-56
 9-31  Price History:  Molybdenum	9-57
 9-32  Industry Characteristics:  Molybdenum	   9-58
 9-33  Molybdenum Ore Processing Plants	9-59
 9-34  Product Uses:  Silver 	   9-61
 9-35  Price History:  Silver	..' .   9-62
 9-36  Production Profile:  Silver 	   9-63
 9-37  Industry Characteristics:  Silver 	   9-64
 9-38  Silver Ore Processing Plants	9-65
 9-39  Product Uses:  Titanium  	   9-69
 9-40  Production Profile:  Titanium	 .   9-70
 9-41  Industry Characteristics:  Titanium	   9-71
 9-42  Titanium/Zirconium Ore Processing Plants	9-72
 9-43  Price History:  Titanium	   9-73
 g_44  Product Uses:  Tungsten  	   9-76
 9-45  Price History:  Tungsten	9-77
 9-46  Industry Characteristics:  Tungsten 	   9-78
 9-47  Tungsten Ore  Processing  Plants	: . .   9-79
 9-48  Production Profile:  Tungsten  	   9-80
                                    xx

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Table
 No.                                                                  Page
 9-49  Product Uses:  Uranium	9-82
 9-50  Industry Characteristics:  Uranium	9-83
 9-51  Uranium Ore Processing Plants 	  9-84
 9-52  Production Profile and Price History:  Uranium	9-88
 9-53  Product Uses:  Zinc	9-90
 9-54  Price History:   Zinc.	9-91
 9-55  Production Profile:  Zinc	  9-92
 9-56  Industry Characteristics:  Zinc	9-93
 9-57  Production Profile:  Zirconium	9-95
 9-58  Price History:   Zirconium .  . .  .	9-96
 9-59  Product Uses:  Zirconium	9-97
 9-60  Industry Characteristics:  Zirconium. .  .	  9-98
 9-61  Strategic Stockpiles.	9-99
 9-62  Summary of Price Increase for the  Most Stringent Regulatory
       Alternative	9-104
 9-63  Summary of Industry Annualized Cost for the Most Stringent
       Regulatory Alternative	  9-127
                                   xxi

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                            LIST OF FIGURES
Figure
 No.
 3-1
 3-2
 3-3
 3-4
 3-5
 3-6
 3-7
 3-8
 3-9
 3-10
 3-11
 3-12
 3-13
 4-1
 4-2
 4-3

 4-4

 4-5
Blake jaw crusher	
Reduction gyratory crusher 	
Fairmount single-roll crusher. ....  	
Hammer crusher 	
Fluid-energy mill. .  	
Grinding systems	
Grizzly bar screen	.,	
Symons 4- by 8-foot double-deck vibrating screens.
Revolving trommel	
Feeders for bulk materials	 .  .  .
Bucket elevator types	
Rotary dryer 	
Rotary kiln	
Types of filtering systems 	
Baghouse cleaning methods.	
Inlet loadings to baghouses in the metallic .and nonmetallic
minerals processing industries 	
Particulate emissions from baghouses at metallic mineral
processing operations. . . 	 	
Particulate emissions from baghouses at nonmetallic
minerals processing operations 	
Page
3-14
3-16
3-20
3-22
3-24
3-26
3-32
3-32
3-35
3-38
3-43
3-46
3-47
4-6
4-7

4-13

4-14

4-15
                                  xxii

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Figure
 No.

 4-6


 4-7


 4-8


 4-9


 4-10


 4-11


 4-12


 4-13


 4-14


 4-15


 4-16

 4-17


 4-18



 4-19


 4-20


 4-21
Particle size distribution for inlet and outlet streams
for baghouse Gl	

Particle size distributions for inlet and outlet streams
at baghouse G2	

Particle size distribution for inlet streams to
baghouse II	

Particle size distribution for inlet streams at baghouse
Jl (primary crusher) and J2 (primary screen) ......
Particle size distribution for inlet stream to
baghouse 01	
Particle size distribution for inlet stream to
baghouse PI	
Particle size distribution for inlet stream to
baghouse P2	
Particle size distribution for the inlet stream to
baghouse Ql	
Particle size distribution for the inlet stream to
baghouse Q2	
Generalized depiction of a dynamic or mechanically-aided
wet scrubber		
Generalized depiction of a venturi  scrubber.
Inlet loadings to wet scrubbers Al through C2 in the
metallic minerals processing industry	
Inlet loadings to wet scrubbers C4 through HI in the
metallic minerals processing industry (note scale change
from Figure 4-23)	
Particulate emissions from low energy wet scrubbers at
metallic minerals processing operations.  .  	
Particle size distribution for inlet and outlet streams
at wet scrubber Al	
Particle size distribution for inlet and outlet streams
at wet scrubber A2 	
Page


4-17


4-18


4-20


4-21


4-24


4-25


4-26


4-28


4-29


4-33

4-34


4-36



4-37


4-39


4-40


4-41
                                  xx tn

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Figure
 No.
 4-22

 4-23

 4-24

 4-25

 4-26

 4-27

 4-28
 4-29
 4-30

 4-31
 4-32
 4-33
 4-34
 6-1

 6-2
 6-3
 6-4
 6-5
 6-6
 6-7
Particle size distribution for the inlet streams  to  wet
scrubber Bl with and without wet suppression 	
Particle size distribution for the outlet stream from wet
scrubber Bl	•  •  •
Particle size distribution for inlet and outlet streams  at
wet scrubber B2	
Particle size distribution for the inlet and outlet streams
at wet scrubber B3 	  	
Particle size distribution for the inlet streams at wet
scrubbers Cl, C2, and C4	•
Particle size distribution for the inlet streams to wet
scrubber Dl	
Methods of hooding conveyor transfer points.
Typical exhaust system for a primary crusher
Typical exhaust system for a secondary or tertiary
crusher	
Screening exhaust systems	
Storage area exhaust systems 	
Product loadout facility exhaust system.
Standard two-stage precipitator	
Inclusive metallic mineral processing industry model
plant	•  •
Aluminum ore processing industry model plant
Aluminum model plant plot plans	
Copper ore processing industry model plant  .
Copper model plant plot plans	 .  .
Gold ore processing industry model plant
Gold model plant plot plans	
Page

4-43

4-44

4-45

4-47

4-48

4-51
4-63
4-65

4-66
4-68
4-69
4-71
4-77

6-3
6-18
6-20
6-25
6-27
6-31
6-33
                                  xxiv

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Figure
 No.
 6-8   Iron ore processing industry model  plant 	    6-38
 6-9   Iron model  plant plot plans	    6-40
 6-10  Lead/zinc ore processing industry model  plant	    6-44
 6-11  Lead/zinc model plant plot plans 	    6-46
 6-12  Molybdenum ore processing industry model plant	  .    6-50
 6-13  Molybdenum model plant plot plans	    6-52
 6-14  Silver ore processing industry model plant 	    6-56
 6-15  Silver model plant plot plans	    6-58
 6-16  Titanium/zirconium sand type ore processing industry
       model plant.	    6-62
 6-17  Titanium/zirconium sand type ore model plant plot plans. .  .    6-64
 6-18  Tungsten ore processing industry model plant 	    6-67
 6-19  Tungsten model plant plot plans	    6-69
 6-20  Uranium ore processing industry model plant	    6-73
 6-21  Uranium model  plant plot plans	    6-75
                                    xxv

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                                 1.   SUMMARY

     Standards of performance for new stationary sources are established
under Section 111 of the Clean Air Act (42 U.S.'C.  7411), as amended in
1977.  Section 111 directs the Administrator of the EPA to establish
standards of performance for any category of new stationary source of
pollution that "...causes or contributes significantly to, air pollution
that may reasonably be anticipated to endanger public health or welfare."
These standards of performance apply to "new stationary sources" defined
as "any stationary source, the construction, reconstruction, or
modification of which is commenced after the publication of regulations
(or, if earlier, proposed regulations)" and must reflect the degree of
emission reduction achievable through application of the best demonstrated
technological system of continuous emission reduction as determined by
the Administrator.                           ,,.
     This Background Information Document (BID) analyzes the impacts of
standards development for the control of particulate emissions from the
metallic mineral processing industry.  Covered by this BID are operations
that process ores of the following metals:
                    Aluminum                 Silver
                    Copper                   Titanium
                    Gold                     Tungsten
                    Iron                     Uranium
                    Lead                     Zinc
                    Molybdenum               Zirconium
     For purposes of analyzing the environmental, economic, and energy
impacts, the process equipment at a metallic mineral processing plant
has been grouped to form the following process units:

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     A.  Crushing unit (primary, secondary, and tertiary) - which is
defined as a crusher and its associated dumping station, grizzly, screens,
coarse ore storage bins, and conveyor belt transfer points.
     B.  Ore storage unit - which is defined as an enclosed ore storage
area and associated conveyor belt transfer points if the bins are
isolated from the crushing unit.
     C.  Dryer unit - including the dryer and associated conveyor belt
transfer points.
     D.  Product loadout unit - including all packaging, product bins,
conveyor belt transfer points, and loadout mechanisms excluding ship
loading facilities.
All new metallic mineral plants will contain some if not all of the
process units listed above.
     Many new metallic mineral plants are expected to recover byproduct
metals or concentrates.   Most metallic mineral processes such as crushing
of ore, operate irrespective of the recovery of byproducts; however,
final processing steps for byproducts or coproducts may involve only
these byproducts.  All processing units, whether associated with the
primary products, byproducts alone, or combinations of these products,
should be considered.
1.1  REGULATORY ALTERNATIVES
     In developing the regulatory alternatives, worst-case uncontrolled
emission characteristics (particulate loading and particle size) were
assumed for all process units at all model plants.  Measurements at
inlets to scrubbers and baghouses tested during this project indicate
that many process units will not have these worst-case characteristics;
however, to ensure that the recommended standard can be met in all
cases, the worst-case particulate loading and particle size assumptions
have been retained.  Furthermore, high-moisture conditions for all
process units in each regulatory alternative have been incorporated
although such high-moisture cases are expected to be limited to some
dryers and a few of the crushers that process ore from underground
mines.  Again, because it is possible that such conditions could occur,
and because we cannot accurately predict the frequency of such
                                 1-2

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conditions in the metallic minerals processing industries, these
conditions have been assumed for all models for the purposes of analysis.
Therefore, the estimated environmental, economic, and energy impacts are
somewhat overstated; however, these overstatements are consistent in
their bases for all regulatory alternatives.
     The following regulatory alternatives were selected for analysis:
     1.   Regulatory Alternative 1 requires no additional standards.
This alternative assumes the use of low energy (1.5-kPa (6-inch water
gauge) pressure drop) wet scrubbers to meet emission levels required by
State Implementation Plans (SIP).   This alternative would result in no
further reduction in emissions at new plants by 1985.
     Test data indicate that current controlled emission rates at existing
facilities are often significantly less than those required by SIP
regulations and these lower emission levels are used as the baseline
control  level.  Fractional efficiency curves for a 6-inch pressure drop
dynamic wet scrubber indicate that under worst-case conditions the
achievable emission level would be about 0.35 g/dscm (0.15 gr/dscf).
     2.   Regulatory Alternative 2 assumes the use of a medium energy
(3.75-kPa (15-inch water gauge) pressure drop) wet scrubber and would
result in an emission reduction of 60 percent over Alternative 1.
Performance evaluations using a programmed scrubber model indicate that
the 15-inch pressure drop scrubber is capable of reducing the worst-case
uncontrolled emissions level to 0.14 g/dscm (0.06 gr/dscf).
     3.   Regulatory Alternative 3 assumes the use of either a high
energy (7.5-kPa (30-inch pressure drop)) wet scrubber or a baghouse and
would result in an emission reduction of 87 percent over Alternative 1.
Source test data indicate that a baghouse will reduce the worst-case
uncontrolled emissions to a controlled level less than 0.05 g/dscm
(0.02 gr/dscf).
     Because of high moisture conditions, standard baghouses may not be
applicable to all emission points.  In these cases, insulated and heated
baghouses or wet scrubbers may be preferred.  Comparative control effi-
ciency evaluations using a programmed scrubber model indicate that a
30-inch pressure drop venturi scrubber would achieve an emission limit
of 0.05 g/dscm (0.02 gr/dscf) under worst-case conditions.  High
                                 1-3

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moisture conditions are expected only for some dryers and a few of the
crushers that crush ore from underground mines.
     Emphasis on worst-case conditions and the design of control equip-
ment to handle worst case conditions should not be interpreted as a
recommendation or a requirement that certain types of equipment would be
necessary to meet a specific emission level under all conditions found
in the metallic mineral industries.   The selection of control equipment
for an actual emissions source requires consideration of the characteris-
tics of only that source.   Rather, the discussions of worst-case
conditions are based on two premises.  First, if an emission level can
be demonstrated as achievable under worst-case conditions, then it is
achievable under all conditions found in the industry.  Second, if the
cost of achieving an emission level is based on the cost of control
equipment designed to meet that emission limit under worst-case conditions,
then the actual cost of control equipment designed to meet the
emission level under less than worst-case conditions should be less.
1.2  ENVIRONMENTAL IMPACT AND ENERGY IMPACTS
     The beneficial and adverse environmental impacts associated wth the
three regulatory alternatives are presented in this section (see Table 1-1),
These impacts are outlined in Chapter 7 and are based on an estimated
25 new plants for the industry to be built prior to 1985.
     Regulatory Alternative 1 would have no additional impact on the
industry or its emissions.  This alternative requires no additional
control measures other than those now being implemented under the appli-
cable SIP regulations.  It is anticipated that if no further standards
are promulgated, new plants would continue to apply control techniques
upon which Regulatory Alternative 1 is based.
     Regulatory Alternative 2 has the potential of reducing annual
particulate emissions from the industry to 8,200 Mg (9,000 tons) for
1985.  This reduction is accompanied by a negligible water impact because
it would cause less than a 1 percent increase in water discharged compared
with a metallic mineral processing plant with baseline control levels.
Additional energy requirements resulting from Alternative 2 are minor
                                 1-4

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and range from a 0.01 percent increase for alumina plants to a 1.6 percent
for titanium/zirconium plants.
     Regulatory Alternative 3 has the potential of reducing the industry's
annual particulate emissions in 1985 by a total of 11,800 mg (13,000 tons)
regardless of which control option is adopted.  Because a baghouse is a
dry collection process, this control option will have no water impact.
The water impact from the use of high energy scrubbers to meet this
alternative is comparable with the impact from Regulatory Alternative 2
and is insignificant.
     The incremental increase in energy use will be the greatest for
Regulatory Alternative 3 using a 30-inch pressure drop wet scrubber.
This increase ranges from 0.04 percent for aluminum plants to 7 percent
for titanium/zirconium plants.  These energy impacts are based on a
comparison of the energy usage of 30-inch pressure drop scrubbers with
the energy consumption of the entire mineral processing operation
(including mining and beneficiation operations with the exception of
pelletizing and calcining operations) with baseline control.  These
impacts are worst-case projections from the standpoint of control equip-
ment energy use because it is extremely unlikely that any plants will
use only 30-inch pressure drop scrubbers.   Rather, it is likely that
most installations will include baghouses for unit processes without
moisture concerns and wet scrubbers (often with less than 30-inch pressure
drop) for unit processes with moisture concerns.  The use of baghouses
may decrease energy use compared with the requirements of low energy
scrubbers.   This positive impact results from the use of more efficient
fans in a baghouse for a given air flow rate as well as the fact that
baghouses do not need pumps to handle scrubber liquids.  Solid-waste
impacts under Regulatory Alternative 3 will be comparable with the
impacts from Regulatory Alternative 2 and are insignificant in
comparison with the tailings from the beneficiation processes.
     Because the particulate matter emitted from lead ore processors
would be expected to contain various amounts of lead, an additional
concern for lead ore processors is the maintenance of the National
Ambient Air Quality Standard (NAAQS) for lead in the vicinity of these
plants.  In the absence of any New Source Performance Standard (NSPS) for
                                 1-6

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metallic mineral plants, new lead ore processing facilities may be
required to meet more stringent emission levels than indicated by typical
State standards for generic particulate matter.  The reduction in particu-
late matter due to the implementation of an NSPS applicable to lead ore
processing plant may be less than indicated in this document because of
a higher level of baseline control required to meet the lead NAAQS.
     Although not expected under most conditions, it could be possible
that, with certain configurations and sitings of new lead ore processing
facilities, a facility could meet the requirements of an NSPS for metallic
mineral processing plants and yet cause a violation of the NAAQS for lead
in the vicinity of this plant.  In this case, a lead ore processing plant
could be required to apply more effective control systems than would be
necessary to meet an NSPS for metallic mineral processing plants.
1.3  ECONOMIC IMPACT
     An economic impact assessment is reported in Section 9.2 for
Regulatory Alternative 3 using the annualized cost for high energy wet
scrubbers.  This control option has the potential for the largest economic
impact of any of the alternatives or control options being considered.
Two parameters are considered by this economic analysis as a means of
quantifying the potential impact.  These parameters are the percentage
increase in the price of the finished product and the percentage increase
in capital expenditures that would be attributable to the use of high
energy wet scrubbers.  The range of price increases for the industry is
from <0.1 percent for the product of aluminum plants to 1.7 percent for
the product of small copper plants.  The increase for small copper
plants is a worst-case impact because the likely recovery of byproduct
metals was not included in the profitability of these operations.  The
installation of control equipment to meet the emission levels of Regula-
tory Alternative 3 will cause an increase in the capital requirements
for new plants ranging from less than 0.1 percent for alumina (bauxite)
plants to 1 percent for a small  (23 megagram (25 ton) per hour) tungsten
plant.  Thus, none of the metallic mineral processing operations covered
by this BID will experience a significant economic impact.
                                 1-7

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     Because of the NAAQS for lead, lead ore processing plants may be
required to apply more effective (and, presumably, more expensive)
control systems than would be required by the State Implementation Plans
(SIP's) for attaining the NAAQS for generic particulate matter.   Thus,
the actual incremental costs (that is the costs above baseline control)
incurred by lead ore processing plants in meeting an NSPS for metallic
mineral processing plants could be less than those presented in this
document.
                                 1-9

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                             2.  INTRODUCTION

2.1  BACKGROUND AND AUTHORITY FOR STANDARDS
     Before standards of performance are proposed as a Federal regulation,
air pollution control methods available to the affected industry and the
associated costs of installing and maintaining the control equipment are
examined in detail.  Various levels of control based on different
technologies and degrees of efficiency are expressed as regulatory
alternatives.  Each of these alternatives is studied by EPA as a
prospective basis for a standard.  The alternatives are investigated in
terms of their impacts on the economics and well-being of the industry,
the impacts on the national economy, and the impacts on the environment.
This document summarizes the information obtained through these studies
so that interested persons will be able to see the information considered
by EPA in the development of the proposed standard.
     Standards of performance for new stationary sources are established
under Section 111 of the Clean Air Act (42 U.S.C. 7411) as amended,
hereinafter referred to as the Act.  Section 111 directs the Administrator
to establish standards of performance for any category of new stationary
source of air pollution which "causes, or contributes significantly to,
air pollution which may reasonably be anticipated to endanger the public
health or welfare."
     The Act requires that standards of performance for stationary
sources reflect "the degree of emission reduction achievable which
(taking into consideration the cost of achieving such emission reduction,
and any nonair quality health and environmental impact and energy
requirements) the Administrator determines has been adequately
demonstrated for that category of sources."  The standards apply only to
stationary sources whose construction or modification commences after
regulations are proposed by publication in the Federal Register.

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     The 1977 amendments to the Act altered or added numerous provisions
that apply to the process of establishing standards of performance.
     1.  EPA is required to list the categories of major stationary
sources that have not already been listed and,regulated under standards
of performance.  Regulations must be promulgated for these new categories
on the following schedule:
     a.   25 percent of the listed categories by August 7, 1980.
     b.   75 percent of the listed categories by August 7, 1981.
     c.   100 percent of the listed categories by August 7, 1982.
A governor of a State may apply to the Administrator to add a category
not on the list or may apply to the Administrator to have a standard of
performance revised.
     2.  EPA is required to review the standards of performance every
4 years and, if appropriate, revise them.
     3.  EPA is authorized to promulgate a standard based on design,
equipment, work practice, or operational procedures when a standard
based on emission levels is not feasible.
     4.  The term "standards of performance" is redefined, and a new
term "technological system of continuous emission reduction" is defined.
The new definitions clarify that the control system must be continuous
and may include a low-polluting or nonpolluting process or operation.
     5.  The time between the proposal and promulgation of a standard
under Section 111 of the Act may be extended to 6 months.
     Standards of performance, by themselves, do not guarantee protection
of health or welfare because they are not designed to achieve any
specific air quality levels.  Rather, they are designed to reflect the
degree of emission limitation achievable through application of the best
adequately demonstrated technological system of continuous emission
reduction, taking into consideration the cost of achieving such emission
reduction, any nonair-quality health and environmental impacts, and
energy requirements.
     Congress had several reasons for including these requirements.
First, standards with a degree of uniformity are needed to avoid
situations in which some States may attract industries by relaxing
standards relative to other States.  Second, stringent standards enhance
                                  2-2

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the potential for long-term growth.   Third, stringent standards may help
achieve long-term cost savings by avoiding the need for more expensive
retrofitting if pollution ceilings are reduced in the future.  Fourth,
certain types of standards for coal-burning sources can adversely affect
the coal market by driving up the price of low-sulfur coal or effectively
excluding certain coals from the reserve base because their untreated
pollution potentials are high.  Congress does not intend that new source
performance standards contribute to these problems.  Fifth, the standard-
setting process should create incentives for improved technology.
     Promulgation of standards of performance does not prevent State or
local agencies from adopting more stringent emission limitations for the
same sources.  States are free under Section 116 of the Act to establish
even more stringent emission limits than those established under Section 111
or those necessary to attain or maintain the National Ambient Air Quality
Standards (NAAQS) under Section 110.  Thus, new sources may in some
cases be subject to limitations more stringent than standards of perfor-
mance under Section 111, and prospective owners and operators of new
sources should be aware of this possibility in planning for such facilities.
     A similar situation may arise when a major emitting facility is to
be constructed in a geographic area that falls under the provisions for
prevention of significant deterioration of air quality in Part C of the
Act.  These provisions require, among other things, that major emitting
facilities to be constructed in such areas be subject to best available
control technology:  The term "best available control technology" (BACT),
as defined in the Act, means:
     an emission limitation based on the maximum degree of reduction
     of each pollutant subject to regulation under this Act emitted
     from, or which results from, any major emitting facility,
     which the permitting authority, on a case-by-case basis,
     taking  into account energy, environmental, and economic
     impacts and other costs, determines is achievable for such
     facility through application of production" processes and
     available methods, systems, and techniques, including fuel
     cleaning or treatment or innovative fuel combustion techniques
                                  2-3

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     for control of each such pollutant.  In no event shall
     application of "best available control technology" result in
     emissions of any pollutants which will exceed the emissions
     allowed by any applicable standard established pursuant to
     Sections 111 or 112 of this Act.  (Section 169(3).
     Although standards of performance are normally structured in terms
of numerical emission limits where feasible, alternative approaches are
sometimes necessary.  In some cases, physical measurement of emissions
from a new source may be impractical or exorbitantly expensive.
Section lll(h) provides that the Administrator may promulgate a design
or equipment standard in those cases in which it is not feasible to
prescribe or enforce a standard of performance.  For example, emissions
of hydrocarbons from storage vessels for petroleum liquids are greatest
during tank filling.  The nature of the emissions (high concentrations
for short periods during filling and low concentrations for longer
periods during storage) and the configuration of storage tanks make
direct emission measurement impractical.  Therefore, a more practical
approach to standards of performance for storage vessels has been equip-
ment specification.
     In addition, Section lll(j) authorizes the Administrator to grant
waivers of compliance to permit a source to use innovative continuous
emission control technology.  To grant the waiver, the Administrator
must find (1) a substantial likelihood that the technology will produce
greater emission reductions than the standards require, or an equivalent
reduction at lower economic, energy, or environmental cost, (2) the
proposed system has not been adequately demonstrated, (3) the technology
will not cause or contribute to an unreasonable risk to the public
health, welfare, or safety, (4) the governor of the State where the
source is located consents, and (5) the waiver will not prevent the
attainment or maintenance of any ambient standard.  A waiver may have
conditions attached to ensure that the source will not prevent attainment
of any NAAQS.   Any such condition will have the force of a performance
standard.   Finally, waivers have definite end dates and may be terminated
earlier if the conditions are not met or if the system fails to perform
                                  2-4

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as expected.   In such a case, the source may be given up to 3 years to
meet the standards with a mandatory progress schedule.
2.2  SELECTION OF CATEGORIES OF STATIONARY SOURCES
     Section 111 of the Act directs the Adminstrator to list categories
of stationary sources.  The Administrator "shall include a category of
sources in such list if in his judgment it causes, or contributes signi-
ficantly to, air pollution which may reasonably be anticipated to endanger
public health or welfare."  Proposal and promulgation of standards of
performance are to follow.
     Since passage of the Clean Air Amendments of 1970, considerable
attention has been given to the development of a system for assigning
priorities to various source categories.  The approach specifies areas
of interest by considering the broad strategy of the Agency for imple-
menting the Clean Air Act.  Often, these "areas" are actually pollutants
emitted by stationary sources.  Source categories that emit these pollu-
tants are evaluated and ranked by a process involving such factors  as
(1) the level of emission control (if any) already required by State
regulations, (2) estimated levels of control that might be required from
standards of performance for the source category, (3) projections of
growth and replacement of existing facilities for the source category,
and (4) the estimated incremental amount of air pollution that could be
prevented in a preselected future year by standards of performance for
the source category.  Sources for which new source performance standards
were promulgated or were under development during 1977, or earlier, were
selected on these criteria.
     The Act amendments of August 1977 establish specific criteria to be
used in determining priorities for all major source categories not yet
listed by EPA.  These are (1) the quantity of air pollutant emissions
that each such category will emit or will be designed to emit, (2) the
extent to which each  such pollutant may reasonably be anticipated to
endanger public health or welfare, and  (3) the mobility and competitive
nature of each such category of  sources and the consequent need for
nationally applicable new source  standards of performance.
                                   2-5

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     The Administrator is to promulgate standards for these categories
according to the schedule referred to earlier.
     In some cases, it may not be feasible to immediately develop a
standard for a source category with a high priority.  This situation
might occur when a program of research is needed to develop control
techniques, or because techniques for sampling and measuring emissions
may require refinement.  In developing standards, differences in the
time required to complete the necessary investigation for different
source categories must also be considered.  For example, substantially
more time may be necessary if numerous pollutants must be investigated
from a single source category.  Furthermore, even late in the develop-
ment process, the schedule for completion of a standard may change.  For
example, inability to obtain emission data from well-controlled sources
in time to pursue the development process systematically may force a  -
change in scheduling.  Nevertheless, priority ranking is, and will
continue to be, used to establish the order in which projects are
initiated and resources assigned.
     After the source category has been chosen, the types of facilities
within the source category to which the standard will apply must be
determined.  A source category may have several facilities that cause
air pollution; emissions from these facilities may vary from insignificant
to very expensive to control.  Economic studies of the source category
and of applicable control technology may show that air pollution control
is better served by applying standards to the more severe pollution
sources.  For this reason, and because there is no adequately demon-
strated system for controlling emissions from certain facilities,
standards often do not apply to all facilities at a source. For the same
reasons, the standards may not apply to all air pollutants emitted.
Thus, although a source category may be selected to be covered by a
standard of performance, all pollutants or facilities within that source
category might not be covered by the standards.
2.3  PROCEDURE FOR DEVELOPMENT OF STANDARDS OF PERFORMANCE
     Standards of performance must (1) realistically reflect best
demonstrated control practice, (2) adequately consider the cost, the
                                  2-6

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nonair-quality health and environmental impacts, and the energy require-
ments of such control, (3) be applicable to existing sources that are
modified or reconstructed as well as to new installations, and (4) meet
these conditions for all variations of operating conditions being
considered anywhere in the country.
     The objective of a program for developing standards is to identify
the best technological system of continuous emission reduction that has
been adequately demonstrated.  The standard-setting process involves
three principal phases of activity:  (1) information gathering,
(2) analysis of the information, and (3) development of the standard of
performance.
     During the information-gathering phase, industries are queried
through a telephone survey, letters of inquiry, and plant visits by EPA
representatives.  Information is also gathered from many other sources,
and a literature search is conducted.  From the knowledge acquired about
the industry, EPA selects certain plants at which emission tests are
conducted to provide reliable data that characterize the pollutant
emissions from well-controlled existing facilities.
     In the second phase of a project, the information about the industry
and the pollutants emitted is used in analytical studies.  Hypothetical
"model plants" are defined to provide a common basis for analysis.  The
model plant definitions, national pollutant emission data, and existing
State regulations governing emissions from the source category are then
used in establishing "regulatory alternatives."  These regulatory
alternatives are essentially different levels of emission control.
     EPA conducts studies to determine the impact of each regulatory
alternative on the economics of the industry and on the national economy,
on the environment, and on energy consumption.  From several possibly
applicable alternatives, EPA selects the single most plausible regulatory
alternative as the basis for a standard of performance for the source
category under study.
     In the third phase of a project, the selected regulatory alternative
is translated into a standard of performance, which, in turn, is written
in the form of a Federal regulation.  The Federal regulation, when
applied to newly constructed plants, will limit emissions to the levels
indicated in the selected regulatory alternative.
                                  2-7

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     As early as is practical in each standard-setting project,  EPA
representatives discuss the possibilities of a standard,  and the form it
might take with members of the National Air Pollution Control  Techniques
Advisory Committee.  Industry representatives and other interested
parties also participate in these meetings.
     The information acquired in the project is summarized in the
background information document (BID).  The BID, the standard, and a
preamble explaining the standard are widely circulated to the industry
being considered for control, environmental groups, other government
agencies, and offices within EPA.  Through this extensive review process,
the viewpoints of expert reviewers are considered as changes are made to
the documentation.
     A "proposal package" is assembled and sent through the offices of
EPA Assistant Administrators for concurrence before the proposed standard
is officially endorsed by the EPA Administrator.  After being approved
by the EPA Administrator, the preamble and the proposed regulation are
published in the Federal Register.
     As a part of the Federal Register announcement of the proposed
regulation, the public is invited to participate in the standard-setting
process.  EPA invites written comments on the proposal and also holds a
public hearing to discuss the proposed standard with interested parties.
All public comments are summarized and incorporated into a second volume
of the BID.  All information reviewed and generated in studies in support
of the standard of performance is available to the public in a "docket"
on file in Washington, D.C.
     Comments from the public are evaluated, and the standards of
performance may be altered in response to the comments.
     The significant comments and EPA's position on the issues raised
are included in the "preamble" of a promulgation package, which also
contains the draft of the final regulation.  The regulation is then
subjected to another round of review and refinement until it is approved
by the EPA Administrator.  After the Administrator signs the regulation,
it is published as a "final  rule" in the Federal Register.
2.4  CONSIDERATION OF COSTS
     Section 317 of the Act  requires an economic impact assessment with
respect to any standard of performance established under Section 111 of
                                  2-8

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the Act.   The assessment is required to contain an analysis of (1) the
costs of compliance with the regulation, including the extent to which
the cost of compliance varies depending on the effective date of the
regulation and the development of less expensive or more efficient
methods of compliance, (2) the potential inflationary or recessionary
effects of the regulation, (3) the effects the regulation might have on
small business with respect to competition, (4) the effects of the
regulation on consumer costs, and (5) the effects of the regulation on
energy use.  Section 317 also requires that the economic impact assessment
be as extensive as practicable.
     The economic impact of a proposed standard upon an industry is
usually addressed both in absolute terms and in terms of the control
costs that would be incurred as a result of compliance with typical,
existing State control regulations.  An incremental approach is necessary
because both new and existing plants would be required to comply with
State regulations in the absence of a Federal standard of performance.
This approach requires a detailed analysis of the economic impact from
the cost differential that would exist between a proposed standard of
performance and the typical State standard.
     Air pollutant emissions may cause water pollution problems, and
captured potential air pollutants may pose a solid waste disposal problem.
The total environmental impact of an emission source must, therefore, be
analyzed and the costs determined whenever possible.
     A thorough study of the profitability and price-setting mechanisms
of the industry is essential to the analysis so that an accurate estimate
of potentially adverse economic impacts can be made for proposed standards.
It is also essential to know the capital requirements fpr pollution
control systems already placed on plants so that the additional capital
requirements necessitated by these Federal standards can be placed in
proper perspective.  Finally,  it is necessary to assess the availability
of capital to provide the additional control equipment needed to meet
the standards of performance.
2.5  CONSIDERATION OF ENVIRONMENTAL IMPACTS
     Section 102(2)(C) of the  National  Environmental Policy Act (NEPA)
of 1969 requires Federal agencies to prepare detailed environmental
                                  2-9

-------
impact statements on proposals for legislation and other major Federal
actions significantly affecting the quality of the human environment.
The objective of NEPA is to build into the decisionmaking process of
Federal agencies a careful consideration of all environmental aspects of
proposed actions.
     In a number of legal challenges to standards of performance for
various industries, the United States Court of Appeals for the District
of Columbia Circuit has held that environmental impact statements need
not be prepared by the Agency for proposed actions under Section 111 of
the Clean Air Act.  Essentially, the Court of Appeals has determined
that the best system of emission reduction requires the Administrator to
take into account counter-productive environmental effects of a proposed
standard, as well as economic costs to the industry.  On this basis,
therefore, the Court established a narrow exemption from NEPA for EPA
determination under Section 111.
     In addition to these judicial determinations, the Energy Supply and
Environmental Coordination Act (ESECA) of 1974 (PL-93-319) specifically
exempted proposed actions under the Clean Air Act from NEPA requirements.
According to Section 7(c)(l), "no action taken under the Clean Air Act
shall be deemed a major Federal action significantly affecting the
quality of the human environment within the meaning of the National
Environmental Policy Act of 1969." (15 U.S.C. 793(c)(l))
     Nevertheless, the Agency has concluded that the preparation of
environmental impact statements could have beneficial effects on certain
regulatory actions.  Consequently, although not legally required to do
so by Section 102(2)(C) of NEPA, EPA has adopted a policy requiring that
environmental impact statements be prepared for various regulatory
actions,  including standards of performance developed under Section 111
of the Act.   This voluntary preparation of environmental impact statements,
however,  in no way legally subjects the Agency to NEPA requirements.
     To implement this policy, a separate section in this document is
devoted solely to an analysis of the potential environmental impacts
associated with the proposed standards.  Both adverse and beneficial
impacts in such areas as air and water pollution, increased solid waste
disposal, and increased energy consumption are discussed.
                                  2-10

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2.6  IMPACT ON EXISTING SOURCES
     Section 111 of the Act defines a new source as "any stationary
source, the construction or modification of which is commenced" after
the proposed standards are published in the Federal Register.   An
existing source is redefined as a new source if "modified" or
"reconstructed" as defined in amendments to the general provisions of
Subpart A of 40 CFR Part 60, which were promulgated in the Federal
Register on December 16, 1975 (40 FR 58416).
     Any physical or operational change to an existing facility which
results in an increase in the emission rate of any pollutant for which a
standard applies is considered a modification.  Reconstruction, on the
other hand, means the replacement of components of an existing facility
to the extent that the fixed capital cost exceeds 50 percent of the cost
of constructing a comparable entirely new source and that it be
technically and economically feasible to meet the applicable standards.
In such cases, reconstruction is equivalent to a new construction.
     Promulgation of a standard of performance requires States to
establish standards of performance for existing sources in the same
industry under Section lll(d) of the Act if the standard for new sources
limits emissions of a designated pollutant (i.e., a pollutant for which
air quality criteria have not been issued under Section 108 or which has
not been listed as a hazardous pollutant under Section 112).  If a State
does not act, EPA must establish such standards.  General provisions
outlining procedures for control of existing sources under Section lll(d)
were promulgated on November 17, 1975, as Subpart B of 40 CFR Part 60
(40 FR 53340).
2.7  REVISION OF STANDARDS OF PERFORMANCE
     Congress was aware that the level of air pollution control achievable
by any industry may improve with technological advances.  Accordingly,
Section 111 of the Act provides that the Administrator "shall, at least
every 4 years, review and, if appropriate, revise" the standards.
Revisions are made to ensure that the standards continue to reflect the
best systems that become available in the future.  Such revisions will
not be retroactive but will apply to stationary sources constructed or
modified after the proposal of the revised standards.
                                  2-11

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              3.   THE METALLIC MINERAL PROCESSING INDUSTRY

3.1  INTRODUCTION
     The source category, metallic mineral processing, has been ranked
number 14 on the EPA list for standards of performance for the control
of air emissions pursuant to Section 111 of the Clean Air Act.  Metallic
mineral processing typically involves the size reduction of ore and the
subsequent separation of the desired mineral or metal from the associated
gangue by one of several possible concentration steps.  Size reduction
operations involve dry and wet crushing and grinding of the ore.  Dry
crushing is a significant source of particulate emissions and will be
discussed extensively in this chapter.  Wet grinding processes and wet
mineral-separation steps do not generate particulate emissions and will
be discussed only briefly.  The drying of the products of the concentra-
tion process, and the various transfer, storage, and loading operations
are sources of particulate emissions and also will be discussed in this
chapter.
     Several sources of particulate emissions in metallic mineral processing
industries will not be covered in this description or elsewhere in this
background document.  Given the possible hazards associated with radioactive
emissions, the emissions from uranium process dryers and from the handling
of uranium processing product (yellowcake) will be evaluated by the
Office of Radiation Programs and, if appropriate, covered by a National
Emission Standard for Hazardous Air Pollutants (NESHAP) for radionuclides.
Ship loading and unloading of metallic minerals are not discussed in
this document due to the somewhat limited demonstration of technology
for controlling emissions from ship holds during these operations for
the metallic minerals of concern and the numerous ship/dock configurations.

-------
In addition, new processing facilities that would be expected to utilize
shipping operations often require the irregular use of noncompany-owned
vessels, and these ships would require substantial retrofitting to
incorporate any new control technology.  In contrast, control techniques
have been widely demonstrated for the dock side conveying and transfer-
ring of material prior to entry into the ship hold or after removal from
the ship hold.  This control technology will be discussed in the section
on ore conveyance.
     Open source fugitive emissions from blasting operations, haul
roads, stockpiles, wastepiles, and tailings ponds are not discussed in ,
this document.  Due to the limited demonstrations of the effectiveness
of specific control techniques and the variety of local conditions,
EPA's Office of Research and Development is currently assessing tech-
niques for the control of open source fugitive emissions.  After these
studies are evaluated, EPA will consider regulation of these sources.
In the interim, open source fugitive emissions are generally regulated
by individual States on a site-by-site basis after consideration of the
local conditions.
     Pyrometallurgical and chemical reaction processes such as concen-
trate roasting and smelting are not discussed in this document but are
covered in other documents (see Environmental Protection Agency 1973,
1974a, 1974b, 1974c, 1974d; Singmaster and Breyer, 1973).  Emissions
from calcining kilns and pelletizing kilns and furnaces are to be
considered in a separate source category.
     Ores of the following metals are the primary metallic minerals
processed in the United States:  aluminum, antimony, beryllium, copper,
gold, iron, lead, molybdenum, nickel, silver, titanium, tungsten, uranium,
vanadium, zinc, and zirconium.  Table 3-1 lists each of these metals,
their ore minerals, chemical composition, and type of gangue.  As shown
in Table 3-1, most metallic ores are composed primarily of nonmetallic
constituents.  The metals and metallic compounds of economic interest
are usually less than 10 percent of the total mined product.  The
only exceptions to this rule are bauxite (20 to 30 percent aluminum)
and iron ore (35+ percent iron).  Thus the particulate emissions from
most metallic mineral processes are composed primarily of nonmetallic
                                 3-2

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constituents.   Although there are other metals produced in the
United States, they were not included if (1) they are primarily bypro-
ducts of the metals in Table 3-1, (2) they are derived from imported
concentrates processed outside the country, or (3) they are covered
under an existing standard (mercury).  Table 3-2 lists these metals and
the reasons for their exclusion from the primary list.  In addition to
metals listed in Table 3-2, the industries processing ores of antimony,
beryllium, nickel, and vanadium will not receive full coverage in this
document because growth in the primary production of these metals is not
expected.  Any growth in the domestic processing of these metallic
minerals will  occur as the byproduction of other metallic minerals
(e.g., nickel  concentrates produced from copper deposits in Minnesota).
     Nineteen states are major producers of one or more processed metal
ores, and eleven states are minor ore producers.  Processing plants vary
from large capacity (> 540 Mg/hr (600 tons/hr)) to small and medium
capacity plants (< 540 Mg/hr).  The distribution of the 200 existing
metallic mineral'processing plants varies greatly by size and number
from one particular industry to another.
     Table 3-3 lists the metallic mineral ores discussed in this docu-
ment and their processing products.  Some of these products may receive
additional processing on site as in some highly integrated copper opera-
tions.  In other cases, these products may be shipped off site for
additional processing by the same manufacturer.  For example, imported
bauxite may be processed into alumina on the Gulf Coast and then shipped
to the Pacific Northwest for final reduction to aluminum metal.  Some of
the products  listed in Table 3-3 may be marketed for other uses as a raw
material or alloying compound (as with molybdenum disulfide or uranium
oxide).  Gold, silver, and antimony are typically processed to a highly
purified state on site before sale or shipment.  Major use categories
for the metals under discussion are given in Table 3-4.
3.2  METALLIC MINERAL PROCESSES OR FACILITIES AND THEIR EMISSIONS
     The objective of mineral processing is to free the metallic minerals
in primary and secondary deposits from mineral(s) of no particular
economic value (gangue).  In general, the major ore processing steps may
include ore unloading, crushing, grinding, screening, concentrating,
                                 3-5

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conveying, mineral separation, ore and product storage, product loading,
and drying.  This section describes individually all processes known
to generate uncontrolled particulate emissions other than those
operations excluded in Section 3.1.
     Although the objective of metallic mineral processing industries
may differ from the objective of many nonmetallic processing industries,
much of the technology in both sets of industries is virtually identical.
Crushing, screening, conveying, storing, and loading operations require
the same consideration in both sets of industries.  The similarity of
these operations was considered in the transfer of emission control
technology from the nonmetallic to the metallic mineral processing
industries as discussed in Chapter 4.
     Because the metallic minerals processing industry is an energy-
intensive industry, considerable research has been devoted to minimizing
energy use.  These concerns are reflected in the design and operation of
the processing plants and equipment.  For example, wet grinding operations
have replaced dry operations in the final milling steps because wet
operations use less energy per unit throughput.  This shift in
technology has an indirect impact in eliminating particle emissions from
this operation.
     Wet size-reduction operations also are used in many operations in
place of more traditional dry secondary and tertiary crushing operations.
The energy impacts of this shift in technology have not been evaluated
fully, particularly the indirect energy cost due to the significant use
of grinding media that are expensive to manufacture.  Thus, the future
technology used in metallic mineral processing is subject to change.
Conceivably, mixed processes will see increased use.  In these systems,
primary crushing (and perhaps secondary crushing) would be dry
operations.  Subsequent size-reduction operations would be wet but would
not be designed to reduce all the ore to the desired size.  The more
resistant portions of the ore would be screened out as oversize and
subsequently sent to a dry crushing operation.
     A conservative approach was taken in the development of this
document.  It was assumed that most size-reduction operations would be
dry as shown in Table 3-5.  If the number of dry operations is
                                 3-9

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overestimated, then the cost of controlling emissions (as developed in
subsequent chapters) will also be overestimated.
3.2.1  Crushing Operations
     Size reduction involves the breaking of large pieces of rock into
intermediate sizes (breaking and crushing) or into fine sizes or powders
(grinding) to meet either maximum or minimum size specifications.  The
ability of a particular ore to withstand size reduction depends upon its
hardness, crystal!ographic structure, and the method(s) used in fracturing
the ore.  Moisture content in the ore is a major factor, especially in
pulverizing operations, because increased moisture content has been
shown to directly correspond to decreased production rates (Perry, 1963,
p. 8-3).
     Because the extent of size reduction by a single machine is limited,
two or more reduction stages are usually necessary.   Crushers are those
machines that break relatively large pieces of rock, and grinding mills
are machines used for comminuting rock into finer sizes. "Primary crushing
typically reduces the ore to a maximum size of 10 to 15 cm (4 to 6 in)
and secondary crushing further reduces the ore to about 3 cm (1 in) in
size.   Tertiary crushing reduces the ore to 1 cm (0.5 in)..
     Rock crushers work by fracturing rock by both compression (rock is
squeezed until it fractures) and impaction (instantaneous breaking
force).  Furthermore, for all crushing processes, attrition (the rubbing
of stone on stone or on metal surfaces) also contributes to size reduction.
Jaw, gyratory, roll, and impact crushers are the four basic types of
crushers used within the industry.
     3.2.1.1  Jaw Crushers.  Jaw crushers work by using approaching and
receding jaws (one movable and one fixed) which use compression forces
to break up the ore.  Jaw crushers are principally used in primary
crushing operations.  The size of a jaw crusher can be defined by its
feed opening dimensions.   These dimensions may range from approximately
8 by 30 cm (3 by 12 in) to 213 by 168 cm (84 by 66 in).   Size reductions
may range from a ratio of 3:1 to 10:1, depending on the nature of the
rock (PEDCo, 1979).   Crusher capacities vary depending on the unit and
its discharge setting.  In general, jaw crushers are run well below
their maximum capacity and run intermittently.
                                 3-12

-------
     There are three main groups of jaw crushers:   (1) the Blake,  which
has a movable jaw pivoted at the top, giving the greatest movement to
the smallest pieces of ore; (2) the Dodge,  which has a movable jaw
pivoted at the bottom, giving the greatest movement to the largest
pieces of ore; and (3) modified combinations of these two methods, which
attempt to give near equal movement to all  sizes of rock (Perry, 1963).
Although there are numerous variations of jaw crushers, they all fall
into two main categories:  (1) variations in toggle motion and
(2) variations in the slope of the crusher jaws.
     The most commonly used jaw crusher is the Blake (double-toggle
type) (see Figure 3-1).  It features an eccentric shaft that drives a
Pitman arm (connecting rod) which raises and lowers a pair of toggle
plates.  The toggle plates activate the opening and closing of the
moving jaw that is suspended from a fixed shaft.  Typically, the jaw
plates are corrugated to assist in gripping the ore.  Table 3-6 lists
the typical operating parameters for jaw crushers.
     3.2.1.2  Gyratory Crushers.  In gyratory crushers, material is fed
into the top of the crusher and is crushed between a rotating head and a
fixed cone.  Gyratory crushers have a much greater capacity than jaw
crushers with equivalent feed openings.  Generally, the crushing rate of
a gyratory crusher depends on the amount of product/size material in the
feed and not the hardness of the material.
     Gyratory crushers can be described in terms of feed opening (A X B
in Figure 3-2), cone diameter (D in Figure 3-2), and the range of open
side discharge settings  (C in Figure 3-2).   For a given feed opening and
cone diameter, crushing  capacity is a direct function of open side
discharge setting.  In primary crushing operations, crushing occurs in
the upper half of the machine and the lower half houses the driving
mechanisms as shown in Figure 3-2.  Gyratories can typically achieve a
size reduction of 6:1 or 7:1 (Richards and Locke, 1940).  Gyratory
crushers operate continuously (some part of the crusher head is working
at all times) and, thus, often are considered to be more advantageous
than jaw crushers because  uniform transmission  of energy is more
economical than  intermittent transmission.
                                  3-13

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            \Vo
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Reduction gyratory  crusher

(Allis-Chalmers  Mfg. Co.).
                             3-16

-------
     Table 3-7 provides operating data for gyratory crushers.   Manufacturers'
listed size designation (column 1 in Table 3-7) refers to dimensions A
and D on Figure 3-2.
     The three basic types of gyratory crushers are:  pivoted-spindle,
fixed-spindle, and cone.  The pivoted- and fixed-spindle crushers are
used for primary crushing; secondary and tertiary crushing is accom-
plished by cone crushers.
     The pivoted-spindle crusher uses a crushing head that is mounted on
a shaft, suspended from above, that is free to pivot.  The bottom of the
shaft is seated in an eccentric sleeve that revolves causing the crusher
head to gyrate in a circular path within a stationary concave circular
chamber.  This action is similar to jaw crushing because in both cases
the crusher element reciprocates to and from a fixed crushing plate.
The crusher setting is determined by the open-side setting at the discharge
end.  This setting is adjusted by raising or lowering the crusher head.
     The fixed-spindle gyratory also has a crushing head mounted on an
eccentric sleeve; however, this is fitted over a fixed shaft.  The full
stroke is exerted on the largest particles as they enter the bowl.
     Cone crushers are used primarily for secondary and tertiary crushing
operations.  Basically, the cone or conical head is gyrated by an eccentric
sleeve driven through gears and a countershaft.  The conical head gyrates
in about the same manner as a primary gyratory crusher, but the cone
covers a greater area and gyrates at a faster rate.  Ore material receives
a series of rapid blows as it passes through the crushing cavity.  Cone
crushers yield a high percentage of fines due to attrition.  The two
most common types of cone crushers are the Symons and the Tel smith.   In
addition to the Symons standard crusher, a Symons short head cone crusher
is available for even greater size reductions.
     3.2.1.3  Roll Crushers.  Roll crushers are generally used in the
final fine-crushing stage or stages of ore processing because they are
better  suited for the production of fine products.
     Roll crushers may  use either single or double  rollers.  The roll
diameters typically range from 0.6 to 2.0 meters (24 to 78 in) and half
narrow  face widths about one-half the size of the roll diameter.  Rolls
may be  either smooth, toothed, or corrugated.  Rock particles, which  are
                                 3-17

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caught between the rolls and crushed, have a reduction ratio of about
3:1 or 4:1 (PEDCo, 1979).   Figure 3-3 depicts a single-roll crusher.
     In a double-roll crusher, two rolls of the same diameter are re-
volved toward each other at identical speeds ranging from 50 to 300
revolutions per minute (rpm).  Usually, one roll moves in fixed bearings
while the other roll has movable bearings.  The distance between the
rolls is adjustable, and springs hold the movable roller to a set clearance
space.
     A single-roll crusher consists of a toothed or knobbed roll and a
curved crushing plate, which may be corrugated or smooth and which
replaces the function of a second roll.  Generally, the crushing plate
is hinged at the top and its setting is maintained by a spring at the
bottom.  Feed is caught between the roll and the crushing plate and is
broken by a combination of compression, impaction, and shear forces at
speeds ranging from 25 to 125 rpm.  Single roll units accept feed sizes
up to 0.51 meters (20 in).  For many purposes, the single roll crusher
is as effective as the larger multiple roll units; however, they are
primarily used for rocks with lower hardnesses (i.e., limestones).
     The capacity of roll crushers is a direct function of the length
and diameter .of the rolls (increasing length and diameter yields in-
creased capacity).  When the rolls are kept full, crushing is accom-
plished not only by the action of the rolls (free crushing) but also by
attrition (choke crushing).  In free crushing, the rolls are fed at a
rate that allows each particle to be crushed and ejected before the next
particle is crushed.  Choke crushing is used in the production of a fine
sized product (if other types of crushers are unsuitable), while free
crushing produces a larger proportion of coarser sizes.  Free crushing
is considered to be more'advantageous because rolls crush by direct
pressure and are usually set to crush a particular size (allowing smaller
particles to drop through without comminution).  This process is noted
for producing a minimum amount of fines.
     3.2.1.4  Impact Crushers.  Impact crushers (including hammer mills
and impactors) use the force of massive impellers or hammers, which
rotate at fast speeds, to shatter free-falling rock particles.  These
units are noted for their high reduction  ratios, and produce a product
that has a wide range of particle sizes and a large proportion of fines.

                                 3-19

-------
       Drive Star
Curved Anvil
    Siedging Crushing
       and Rolls
Pressure equalizing
    Springs
 Figure 3-3.   Fairmount single-roll  crusher
                (Allis-Chalmers  Mfg.  Co.).
                           3-20

-------
     Hammer mills can be used as either primary or secondary crushers,
and are primarily used in metallic ores that have lower hardnesses
(i.e., uranium-containing sandstone and bauxitic clays).   Hammer mills
are used for finer crushing than can be accomplished by roll crushers.
A hammer mill, depicted in Figure 3-4, consists of pivoted hammers
mounted on a horizontal shaft.  Crushing takes place by impact between
the hammers and fixed breaker plates.  In addition, a cylindrical grating
may be positioned beneath the rotor, at the discharge opening, to retain
material until it is reduced to a size small enough to pass between the
base of the grating.  The size of the product can b,e regulated by chang-
ing the spacing of the grate bars and by either lengthening or shortening
the hammers.  As rock particles are fed into the crushing chamber, they
are shattered by the hammers, which may attain peripheral speeds up to
75 meters per second (250 ft/s), and by impact with a steel breaker
plate.  Rotor speeds range from 250 to 1,800 rpm, and capacities may
exceed 900 megagrams per hour (1,000 tons/hr).
     Impact crushers are similar to hammer mills; however, they do not
have grates or, screens ;to restrain crushed rock.  Feed is broken by
impact alone. .,Adjustable breaker bars are used to deflect material back
into the part'of the impellers.  Primary reduction units are available
which can reduce material to about 2.5 centimeters (1.0 in); however,
these units are usually limited to ores of lower hardnesses.  Typical
operating data for impact crushers are presented in Table 3-8.
     3.2.1.5  Fluid Energy Mills.  Fluid energy mills are not used in
the metallic mineral industry because the size reduction accomplished
exceeds that required by most metallic mineral processes.  These mills
are used in the nonmetallic mineral industry, for example, to process
fullers earth clays.  Because emission tests from nonmetallic industries
are included in the data base discussed in Chapter 4, a brief descrip-
tion of this process is necessary.
     When the desired material size is in the range of 1 to 20 micrometers,
an ultrafine grinder such as the fluid energy mill is required.  A
typical fluid energy mill is shown in Figure 3-5.  In this type of mill,
the particles are suspended and conveyed by a high velocity gas stream
                                 3-21

-------
                                   Feed
Breaker Block
                                 Discharge
                       Figure 3-4.  Hammer Mill
Rotor Assembly
                                                           Rotor Size
                                                           (Diameter)
                                    3-22

-------
               Table 3-8.   OPERATING DATA FOR IMPACT CRUSHERS1
     Feed opening
    cm          in
      Capacity range
    Mg/hr      tons/hr
Energy requirements
  kW          hp
 86 x 142    34 x 56
 97 x 160    38 x 63
180 -   315  200 -   350    112 - 186   150 - 250
270 -   540  300 -   600    149 - 298   200 - 400
142 x 234    56 x 92     540 - 1,260  600 - 1,400    298 - 522   400 - 700

aRexnord, Inc., 1975 and 1976c.
                                                                  -s
                                     3-23

-------
Reduction
  Chamber
                                                   Sized
                                                   Particles
   Nozzles
                                                        Heavier
                                                        Particles
                                                        Air or.
                                                        Steam Inlet
                  Figure 3-5.  Fluid-energy mill
                              3-24

-------
in a circular or elliptical path.  Size reduction is caused by impaction
and rubbing against mill walls and by interparticle attrition.  Classification
of the particles takes place at the upper bend of the loop shown in
Figure 3.17.  Internal classification occurs because the smaller particles
are carried through the outlet by the gas stream while the larger particles
are thrown against the outer wall by centrifugal force.  Product size
can be varied by changing the gas velocity through the grinder.
     3.2.1.6  Crushing and Grinding Circuits.  .Size reduction systems
          '*                ft        ;,.'•*'•       \.~  ~ '•
are operated on either a batch or a continuous basis.  Most operations
use the continuous method because batch grinding .often produces a product
that is overground.  In addition, batch grinding is less energy efficient
than continuous grinding.  Continuous operations are accomplished using
either an open or closed circuit.  As shown  in Figure 3-6, in a continuous
open circuit the product discharged from a size  reduction operation goes
directly to the next operation.  In a continuous closed circuit, the
discharges,go to a screen  or size classifier that separates the insuf-
ficiently ground portion of the  ore and recycles it to the original
feed.  With the exception  of the coarse grinding stages, where a definite
maximum particle stze is not a major factor, the preferred method is to
use closed circuits.  Even in coarse grinding, the circuit still may be
      •, •  ,  '             "-^            '---•*-
closed by using screens to retain material until it  is the proper size
          .;
for discharge;
3.2.2  Emissions from Crushing Operations
     The primary purpose for reporting emission  factors in this chapter
is to indicate the range of emissions which  might be expected from the
operations  of concern in the metallic minerals processing industry.  The
range of emissions can,be,;  used to indicate the severity of the problems
that may be encountered and .the  suitability  of .various control techniques,
particularly in light of worst case conditions.  These factors should
not be used indiscriminately  in  the calculation  of  emission  levels from
individual  facilities;  however,  we  believe they  are  typical  of the
levels that would  be  found in the industry and thus  may be used in
industry-wide studies as presented  in this document.
     Crushing operations are a major source  of particulate emissions.
Theoretically,  emissions may be  influenced by a  large  number of factors
                                  3-25

-------
      BATCH
CONTINUOUS.
OPEN CIRCUIT
                                                      PRODUCTS
                                          CLASSIFIER
    FEED
                        CONTINUOUS.
                        CLOSED CIRCUIT
                                 MILL
Figure  3-6.   Grinding systems
From Chemical  Engineer's Handbook  by J.  H.  Perry,
1963.  McGraw-Hill  Book Company, Inc,  Used with
the permission of McGraw-Hill Book Company.
                   3-26

-------
that include the moisture content of the rock, the type of rock processed,
the type of crusher employed, the size of the final product (i.e.,
primary, secondary, or tertiary stage) as well as whether the process
uses open- or closed-circuit methods.
     The type of force (impaction, compression, or attrition) exerted on
the raw materials by a particular crushing method could affect the size
distribution of the product.  The amount of fines produced in turn may
affect the amount of emissions.  In addition, the fan-like action produced
by the opening and closing of the jaw mechanisms on jaw crushers might
be expected to produce a higher amount of emissions compared with the
gyratory crushers.
     In general, impact crushers produce a- larger proportion of fines
than compression crushers which reflects the  higher reduction ratios
expected for hammer mills (pulverization) compared with jaw and gyratory
crushers.  In addition to generating more fines, impact crushers also
impart more velocity to the particles because of the fan-like action
produced by the whirling hammers.  For these  reasons,  impact crushers
might be expected  to generate more uncontrolled particulate emissions
per megagram of ore processed than other types of  crushers.
     Uncontrolled  emissions  from jaw, gyratory (including cone),  and
roll crushers might be expected to correspond to the reduction  stage of
the ores.  Basically, the greater the reduction stage  (i.e., tertiary
crushing), the  higher the emissions.
     A  summary  of  factors that might affect  the amount of emissions
generated  by crushing operations  is  presented in Table 3-9.  Little work
has been  done to  date to correlate these factors with  uncontrolled
emission  rates.   For the purposes of designing control equipment, an
uncontrolled emission rate  is  generally assumed to be  12  to 23  grams per
dry normal  cubic  meter  (g/DNm3)  or 5 to 10 grains  per  dry standard cubic
foot  (gr/dscf)  by air emission control  equipment  designers (Skalos,
1980;  Soderberg,  1980).  As will  be  discussed in  Chapter  4, the air  flow
rates  through control equipment  are  most often determined by the size  of
 hood  openings, and the necessity  of  maintaining certain minimum  air  flow
 rates  and velocities  at the hood openings  and in  the ducts rather than
                                  3-27

-------
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                                                    3-28

-------
by considerations of uncontrolled emission rate.   Tests conducted by EPA
and reported in Chapter 4 indicate that uncontrolled emission rates are
generally below 12 g/DNm3 (5 gr/dscf) and often below 2.5 g/DNm3
(1 gr/dscf).  There was some indication in these tests that increased
ore moisture level will lower uncontrolled emission levels; however, the
trend was not entirely clear.  Given the wide variety of conditions
tested, it does not appear likely that any combination of factors that
could theoretically affect uncontrolled emissions rates would result in
an increase in emission levels above design criteria of control equipment
if proper consideration is given to maintaining required air flow rates.
     In addition to the particulate matter concentration from an opera-
tion, the particle size distribution of the uncontrolled emissions can
affect the selection of control equipment.  Generally, the tests described
in Chapter 4 found no difference in the particle size distributions of
emissions by reduction stage (i.e., primary, secondary, tertiary).
Median particle size for emissions from crushing operations was in the
range of 5 to 15 microns.  The use of closed circuits, which allow small
sized ore to bypass a particular reduction step, may also help reduce
the emission of fines.
    • Only when the size reduction operation reduces the processed ore to
a  size range under 50 microns does the particle size distribution of the
uncontrolled emissions obviously reflect  the reduction stage.  A test of
the particle size distribution of the emissions from a fluid energy mill
reported  in Chapter 4  supports this  premise.   In the metallic  mineral
industry  final size reduction  is accomplished  with wet grinding operations.
Thus, the  fine particle size distribution found in the fluid energy mill
is not often expected  in  this  industry, particularly where  high  uncontrolled
emissi ons  are  present.
3.2.3  Screening Operations
      Screening is the  separation  of  a mixture  composed of various  rock
 sizes  into two or more portions  by  a screening surface.   Basically,
material  is dropped onto  a screening surface  that has  openings of  a
 designated size.   Material remaining on  the  screen  surface is  the  oversize
 or "plus"  material; material passing through  the  screen  is the undersize
                                  3-29

-------
or "minus" material.  Multiple screens may be used to divide material
into several successively finer fractions of known particle size distribution.
     Screen sizing can be used to provide a variety of functions in ore
concentration plants.  In crushing operations, screens can be used to
bypass sufficently reduced material from crushing operations.   Screens also
can be used to form a closed circuit in conjunction with crushing machines
to limit the maximum size of the final product; this increases the
capacity and efficiency of the crusher.  Screening can divide crushed
ore into a series of products, each having a limited range of size.
This method grades the ore into separate feed fractions which can be fed
to different machines that are adjusted for the feed size.  This provides
better separations than can be accomplished from unsized feed.  Finally,
for some industries, product size is an essential part of the final0
product specifications, and screening is used for commercial grading to
segregate products meeting certain specifications.
     Screening surfaces may consist of woven wire, perforated or punched
plates, metal bars, or wedge wire sections.  The type of material used
for screens depends on the aperture desired and the nature of the work.
For very heavy coarse material, parallel iron bars or rails may be
employed.  In finer work, punched plates, woven wire or rod screens are
used.  The efficiency of screening operations largely depends on the
rate of screening and on the aperture of the screen.  Typically,  ,
increasing the rate of feed to a screen decreases the screen's efficiency.
Screening efficiency is also dependent upon the size distribution of the
feed and the type of motion imparted to the screen surface.  The efficiency
of screening operations is commonly defined as the ratio of undersize
that passes through screen to the true undersize.  This value is determined
from screen tests and subsequent calculations on the feed and oversize
products.  Screening efficiencies vary widely, and average about 70 to
80 percent (Richards and Locke, 1980).  The two basic types of screens
used in metallic ore dressing are stationary screens, which include some
types of grizzlies, and moving screens, which include shaking screens,
vibrating screens, and revolving screens.
                                 3-30

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     3.2.3.1  Grizzlies.   Grizzlies consist of a set of parallel uniformly
spaced bars, rods, or rails held apart by spacers at a predetermined
opening.  Figure 3-7 depicts a bar screen (grizzly).  Grizzlies may be
placed in either an inclined or horizontal position (usually inclined
between 25 and 39 degrees).  The bars are typically wider on the top
surface than on the underside to ensure free discharge of the undersize
particles.  Spacing between the bars can range from 5 to 20 cm (2 to
8 in).  Grizzlies are usually constructed of manganese steel or other
highly abrasion-resistant materials.  Grizzlies are primarily used to
remove crusher undersize prior to primary crushing operations, thus,
reducing the load on the primary crusher.
     Vibrating grizzlies are simple bar grizzlies mounted on eccentrics
which give the entire assembly a back and forth (oscillating) movement
at approximately 100 strokes a minute.  This promotes a more even flow
through and across the bars.
     3.2.3.2  Shaking Screens.  Shaking screens consist of rectangular
frames which hold either a wire cloth screening surface or a perforated
plate that is slightly inclined and suspended by loose rods or cables,
or suspended from a base frame by flexible flat springs.  The screen is
mechanically shaken parallel to the plane of material flow.  Frequencies..
range from 60 to 800 strokes per minute and amplitudes range from 2 to
23 cm (0.75 to 9.0 in).  They are generally used for screening coarse
material  12 mm (0.5 in) or  larger.
     3.2.3.3  Vibrating Screens.  Vibrating screens are standard when
large capacity and high efficiency  are desired.  They have replaced most
other screening types because of their much greater.capacities.  A
vibrating screen  consists  of an inclined  flat or convex screening sur-
face that is rapidly vibrated in a  plane  normal or  nearly normal to the
screen  surface (see Figure  3-8).  These  vibrations  may be generated
mechanically by an eccentric shaft,  unbalanced  fly  wheel, cam or tappet
assembly, or electrically  by an electromagnet.  Mechanically vibrated
screens are operated at 1,200 to 1,800 rpm and  with amplitudes  of 0.3 to
1.3 cm  (0.3 to 0.5 in).  In general,  the  type of motion imparted to the
particles and the efficiency of the machine depends upon the feed.  For
example,  in medium to coarse sizing a screen  using  an eccentric shaft
would be chosen.

                                 3-31

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         Figure 3-7.   Grizzly bar screen
                       (Richards and Locke, 1940)
Figure 3-8.   Symons 4- by  8-foot double-deck  vibrating screens
              (Richards and Locke,  1940)
                              3-32

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Other variations may be more suitable for finer sized fractions.   Table 3-10
tabulates typical power requirements for vibrating screens.
     3.2.3.4  Revolving Screens, (trommel).  Revolving screens consist of
an inclined cylindrical frame that has a screening surface of wire cloth
or perforated plates wrapped around it.  Feed material is introduced at
the upper end and as the screen rotates, undersized material passes
through the screen openings while oversize material is discharged at the
lower end.  Revolving screens are available up to 1.2 m (4 ft) in diameter,
and usually revolve at 15 to 20 rpm (see Figure 3-9).
3.2.4  Emissions from Screening Operations
     Oust is emitted from screening operations as a result of the agitation
of dry material.  The amount of dust emitted may depend upon the grain
size of the feed, the moisture content of the feed, and the agitation
frequency and amplitude.  In general, screens agitated at large amplitudes
and high frequencies could be expected to emit more dust than those
operated at smaller amplitudes and  lower  frequencies  for equivalent feed
sizes.  In addition, the screening  of fines produces  more emissions, due
to the increase  of dust-sized particles,  than the screening of coarser
feed.  Table 3-11 lists some parameters that affect emissions from
screening operations.                                  ,
     Typical design criteria for control  equipment for screens allow for
emission  rates  of 12 to 23 g/DNm3  (5 to 10 gr/dscf)  (Soderberg, 1980).
Tests of  uncontrolled  emissions from screens (see Chapter 4)  indicate
that rates under 2.5 g/DNm3  (1,0 gr/dscf) are more typical.
3.2.5  Grinding Operations
     Grinding  involves  the reduction of ore material  into particle  sizes
smaller  than those  attainable by crushers.  The  chief purposes of grinding
are  to liberate metallic minerals  from gangue, reduce ore materials  to
sizes meeting  specific process  requirements  (i.e., for chemical beneficia-
tion), and to  produce  particle  sizes meeting commercial  product requirements
(particle size limitations).  Grinding equipment typically  consists  of  a
cylindrical  or conical  shell  that  rotates on a horizontal axis.  The
shell  is charged with  a grinding medium such as  balls of steel, flint  or
porcelain,  or  with  steel  rods.   In some cases, large particles  in the
                                  3-33

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           Table 3-10.   POWER REQUIREMENTS  FOR VIBRATING SCREENS*
Screen
m
0.9 x 3.6
0.9 x 4.8
1.2 x 3.6
1.2 x 4.2
1.2 x 4.8
1.5 x 3.6
1.5 X 4.2
1.5 X 4.8
1.8 x 4.2
1.8 x 4.8
2.1 x 6
2.4 x 4.8
size
ft
3 x 12
3 x 16
4 x 12
4 x 14
4 x 16
5 x 12
5 x 14
5 x 16
6 x 14
6 x 16
7 x 20
8 x 16
Energy
kW
7
7
7
11
11
11
11
15
15
15
15
19
requirements
hp
10
10
10
15
15
15
15
20
20
20
20
25
aDerived from Bixby-Zimmer,  undated;  Rexnord,  1972;  and ATMs-Chalmers, 1977b,
 1975b, and 1973a.
                                    3-34

-------
Figure  3-9.  Revolving trommel
              (Richards and Locke, 1940)
                      3-35

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               Table 3-11.  PARAMETERS FOR SCREENING OPERATIONS
Type of screen
   Rate of screening
Aperture size
 Amplitude
Grizzlies
Shaking screen
Revolving screen
  (trommel)
100 strokes/min
60-80 strokes/min
Vibrating screen     1,200-1,800 strokes/min
8-30 rpm
> 5 cm (2 in)
varies
0.25 mm-250 mm
  (0.01-10 in)
2.5 mm-50 mm
  (0.1-2 in)
stationary
5-58 cm
(2-23 in)
0.3-1.3 cm
(0.1-0.5 in)
NAa
aNA = Not applicable to this method.
 Increase in rate of screening may increase emissions.
°Decrease in aperture size may increase emissions.
 Increase in amplitude may increase emissions.
                                     3-36

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feed material can act as the charge.   The basic types of grinding mills
are rod, ball or pebble, and autogenous or semi autogenous.   As indicated
by their names, these grinding mills use different types of grinding
media.  Autogenous and semi autogenous mills rely either wholly or
partially on the ore itself to serve as the grinding medium.  Grinding
mills may be operated as either wet or dry processes; because wet
grinding operations consume approximately 30 percent less energy than
dry grinding per unit throughput, only wet grinding operations are
expected in the future.
3.2.6  Emissions from Grinding Operations
     Because wet grinding is the preferred technology for future metallic
mineral processing operations, particulate emissions from grinding
operations are not expected.
3.2.7  Conveying Operations
     Handling systems are necessary to transport materials from one
process point to another.  The selection of the correct system for
material of a specific bulk in a particular situation is a very compli-
cated procedure.  Some of the more important factors to be considered in
materials handling are capacity requirements,  length of transport, lift,
material characteristics, and processing requirements.  The most common
systems include feeders, belt conveyors, bucket elevators, screw conveyors,
and pneumatics.  There are two chief classes of conveyors - those that
move  forward with the product (endless conveyors), and those in which
the product  is moved by the propelling motion  of a screw thread or by
the jerking  of an oscillating tube or trough.
      3.2.7.1  Feeders.  Feeders are relatively short, heavy-duty conveying
systems that deliver ore to process equipment  at a predetermined uniform
rate  which can be adjusted to the type of  feed.  The more commonly used
feeders are  the apron, belt, reciprocating plate, vibrating, and wobbler
(see  Figure  3-10).
      Apron feeders consist of overlapping  metal pans  (aprons) that are
hinged  or linked together  by chains to form an endless conveyor  supported
by rollers spaced between  a head and tail  assembly  (PEDCo,  1979).  They
are constructed to withstand high impact and abrasion and are available
in various widths and  lengths.  Special pan plates  are available that
can minimize drop at the discharge point.

                                 3-37

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     Belt feeders are short, heavy-duty conveyors with closely spaced
support rollers.   Adjustable gates are used to regulate feed rates.
Their chief advantage is the elimination of dribble which is a problem
encountered with apron-type feeders.  They are available in 0.4 to 1.8 m
(1.5 to 6 ft) widths and 1 to 8 m (3 to 24 ft) lengths and are operated
at speeds of 12 to 30 m (40 to 100 ft) per minute.
     Reciprocating plate feeders consist of a heavy-duty horizontal
plate driven in a back and forth motion which causes material to move
forward at a uniform rate.  The feed rate is controlled by adjusting the
frequency and length of the strokes.  Reciprocating feeders usually run
between 15 and 40 strokes per minute.  They are more commonly used for
materials that are not seriously abrasive.
     Vibrating feeders consist of a steel pan or feed chute which is
freely supported or suspended and is vibrated electromagnetically in a
direction oblique to its surface (see power requirements, Table 3-12)
(Richards and Locke, 1940).  Material in the pan is moved along the pan
surface by these vibrations, the rate of movement depending on the
amplitude and frequency of the vibration.  In general, vibrating feeders
operate at high frequencies and low amplitudes.  Feed rate is controlled
by the slope of the feeder and the amplitude of the vibrations.
     Wobbler feeders consist of a series of closely spaced elliptical
bars that are mechanically rotated causing oversize material to tumble
forward to the discharge end and undersize material to pass through the
spaces.  The feed rate is controlled by the bar spacing and the speed .of
rotation.
     3.2.7.2  Belt Conveyors.  Belt conveyors are the most widely used
means of material transport, elevating, and handling.  A belt conveyor
consists of an endless belt running on two large pulleys or drums and
with intermediate supporting idlers.  The belts are usually made of
special quality (reinforced) rubber to withstand the wear.  The belt is
stretched between a drive or head pulley and a tail pulley.  Rubber-belt
conveyors usually discharge at one end, but the ore also may be discharged
at any desired point along the side by fixing an oblique scraper or
special trippers (to raise and lower the belt) to the conveyor.  Belt
                                 3-39

-------
      Table 3-12.   POWER REQUIREMENTS FOR
               VIBRATING FEEDERS9
Feeder
m
0.9 x 3.6
0.9 x 4.2
0.9 x 4.8
0.9 x 6
1.1 x 3.6
1.1 x 4.2
1.1 x 4.8
1.1 x 6
1.2 x 3.6
1.2 x 4.2
1.2 x 4.8
1.2 x 6
1.4 x 3.6
1.4 x 4.2
1.4 x 4.8
1.4 x 6
1.5 x 3.6
1.5 x 4.2
1.5 x 4.8
1.5 x 6
1.5 x 7.3
1.8 x 4.2
1.8 x 4.8
1.8 x 6
1.8 x 7.3
size
Energy requirements
ft
3
3
3
3
3.5
3.5
3.5
3.5
4
4
4
4
4.5
4.5
4.5
4.5
5
5
5
5
5
6
6
6
6
x 12
x 14
x 16
x 20
x 12
x 14
x 16
x 20
x 12
x 14
x 16
x 20
x 12
x 14
x 16
x 20
x 12
x 14
x 16
x 20
x 24
x 14
x 16
x 20
x 24
kW
11
11
11
19
11
11
11
19
11
11
11
19
11
11
11
19
11
19
19
22
22
19
22
22
30
hp
15
15
15
25
15
15
15
25
15
15
15
25
15
15
15
25
15
25
25
30
30
25
30
30
40
Data from Allis-Chalmers, 1973b.
                     3-40

-------
conveyors may range from 0.36 to 2.0 m (14 to 80 in) in width, with
operating speeds ranging from 30 to 270 meters/min (100 to 800 ft/min).
Table 3-13 presents' operating parameters for belt conveyors.
     3.2.7.3  Elevators.  Bucket elevators are used when substantial
height differentials are required within a limited space.  In general,
they consist of buckets that are attached to a single- or double-strand
chain or belt that is supported and driven by a head and foot assembly.
The three most common types of bucket elevators are the high-speed
centrifugal discharge, slow-speed positive or perfect discharge, and the
continuous discharge (see Figure 3-11).
     Centrifugal discharge elevators are the most common type.  As the
buckets round the tail pulley, which is housed within a suitable curved
boot, they scoop up their load and elevate it to the point of discharge.
The buckets are spaced to allow the material to discharge by the centri-
fugal action of the buckets when they round the head pulley.  This type
of elevator can handle almost any free-flowing or small lump material.
Speeds can be relatively high for dense materials but must be lowered
for finer sized materials to prevent fanning action.
     Continuous elevators are generally used for larger lump materials
or materials too difficult to handle with centrifugal discharge units.
The gentle discharge makes this type of elevator effective for handling
finely pulverized material.  This method utilizes closely spaced buckets.
The back of the preceding bucket is used as a discharge chute.
     Slow-speed positive elevators are almost identical to the centrifugal
discharge elevators; however, the buckets are mounted on two  strands  of
chain, and are  snubbed  back  under the  head  sprocket to  invert them for
positive discharge  (Perry, 1963).  These units  are  designed especially
for materials that  have a tendency to  pack.   In  extreme  cases,  knockers
may be used to  hit  the  buckets  at the  discharge  point to help free
material.
     3.2.7.4  Screw Conveyors.   Screw  conveyors  are the  most  versatile
of the conveyors.   They consist of  a  steel  shaft with  a spiral  or  helical
fin that, when  rotated, pushes  material  along a trough.  They are  sometimes
used to  convey  finer sized ores.
                                  3-41

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          •DISCHARGE
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Figure  3-11.   Bucket elevator  types
                  3-43

-------
     3.2.7.5  Pneumatic Conveyors.  Pneumatic conveyors consist of tubes
or ducts that convey material by means of a high-velocity airstream or
by vacuum pressure generated by an air compressor.   Generally, for a
given length and capacity, the pneumatic conveyor requires more horse-
power per ton of transported material than mechanical conveyors.  Pneumatic
systems may be advantageous where light or fine material is used.
3.2.8  Emissions from Conveying Operations
     Particulate emissions may be generated from any of the conveying
operations.  The level of uncontrolled emissions depends on the size of
the material handled, the degree of agitation of the material (vibrations),
the belt speed, the moisture content of the material, the free-fall
distance of the material, and the forces imparted to particles at discharge
points (elevators).
     Most of the emissions from material handling occur at transfer
points.  These points include transfers from one conveyor to another, or
discharge of materials into hoppers or storage piles (stockpiles).
Additional emissions may be generated due to climatic factors (wind),
and also some operations, such as pneumatic conveyors, that agitate
material by air flow and may increase the dust level within the system.
     Design criteria for control equipment for transfer points often
allow for uncontrolled emissions at the head of a conveyor transfer
point of 5 to 10 g/DNm3 (2 to 5 gr/dscf) and at the  receiving belt of 10
to 30 g/DNm3 (5 to 15 gr/dscf) (Soderberg, 1980).  Tests of conveyor
transfer points showed typical uncontrolled emissions of less than
2.5 g/DNm3 (1.0 gr/dscf).  At one facility tested, dry bauxite ore with
a high percentage of fine particles is transferred between a boom and a
conveyor belt.  This transfer operation involved a 30-foot free fall.
Uncontrolled emissions of 10.9 g/DNm3 (3.8 gr/dscf)  have been reported
from this transfer point  (Sweet, 1980).
3.2.9  Drying Operations
     Ores containing excess moisture due to wet beneficiation,  climate
factors, or specific rock characteristics must be dried.  Excess moisture
is a major problem that can  result in higher freight charges, frozen
stockpiles or rail cars, and  can pose major difficulties  in subsequent
ore processing stages (i.e., smelting operations).   The  main  types
                                  3-44

-------
 of driers  used  in metallic ores are  rotary,  screw  conveyors, and rotary
 kilns.  As discussed below,  kilns are primarily  used  in  calcining and
 other operations causing  chemical changes.
     3.2.9.1  Rotary Driers.   Rotary driers  are  a  type of machine where
 various materials are  subjected to the  actions of  hot air or hot gases
 from an adjoining furnace tube (Figure  3-12).  The dryer tube  is typically
 mounted at a  small  angle  to  the horizontal of the  kiln.  Moisture is
 released as the material  moves from  one end  of the tube  to  the other as
 the tube is rotated.   Moisture release  is  accomplished by either direct
 heat transfer (heat is added to the  solids by direct  exchange  between
 flowing air or  gas  and the solids) or indirect heat transfer (the heating
 medium is  separated from  physical contact with the solids by a metal
 tube or wall).  Drying of most metallic ores involves direct heat transfer.
 The length of the cylinder may be from  4 to  more than 10 times the
 cylinder diameter,  which  may vary from  less  than 1 to more  than 10  feet.
 Gas or air flowing  through the cylinder may  increase  or  retard the
 •movement of material,  depending on whether the gas or air flow is
.countercurrent  or cocurrent  to the solid flow.
     3.2.9.2  Screw Conveyors. Screw conveyors  can be adapted for
 drying material by  the use of hollow screws  and  pipes which may be
 attached to circulate  hot fluids.  In these  cases, the screw conveyor  is
 sealed from the outside atmosphere.  This  type of  drying operation  is
 used infrequently in the  metallic minerals industry.
     3.2.9.3  Rotary Kilns.   Rotary  kilns  may also be used  to  dry
 materials  although  they are  primarily used in calcining  and roasting
 operations.   They replace ordinary rotary  dryers when the wall
 temperature exceeds 370 to 420°C  (700 to 800°F).  Usually,  they consist
 of  a horizontal furnace that has  a cylindrical body and  conical ends
 lined  in part or  entirely with refractory  material (Figure  3-13).   Feed
 is  introduced to  the  upper part  of the  kiln  by  inclined  chutes, overhung
 screw  conveyors,  etc.   The product then moves through the  kiln and  the
 dried  material  is discharged at  the  lower  end onto conveyors  or cooling
 devices which may include rotating  inclined  cylinders,  shaking grates,
 etc.   Kiln length is  a major factor  in  determining thermal  efficiency.
 Kilns  with a  high ratio of  length to diameter have greater  thermal
 efficiencies  than those with a low ratio.

                                  3-45

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3.2.10  Emissions from Drying Operations
     Because the material being dried is usually agitated in order to
expose more drying surface to the hot air current, significant quantities
of particulate emissions in the exhaust stream from a dryer are possible.
Dryers are typically used to dry the final product of the mineral  processing
operation; thus the value of material leaving the stack could be significant.
Where emissions are high (in excess of 20 to 30 gm/DNn3 (10 to 15 gr/dscf)),
there is usually a financial incentive to install product recovery
devices such as dry cyclones which would reduce the loading to the final
control device.
     Design criteria for control equipment for dryer exhausts are based
on uncontrolled emissions of 12 to 35 g/DNm3 (5 to 15 gr/dscf) (Soderberg,
1980).  Tests reported in Chapter 4 indicate uncontrolled emissions
between 1 and 25 g/DNm3 (0.2 and 10 gr/dscf).  Median particle sizes for
dryers tested in Chapter 4 were between 2 and 10 microns.
3.2.11  Bagging and Bulk Loading Operations
     Processed ore material may be transported by bulk loading or by
bagging to customers.  For materials shipped to a single customer in
annual excess of 4.5 gigagrams (10 million pounds), the most economical
means for both shipper and receiver is bulk shipments.  In these cases,
the carrier (railroad car, truck, or ship) is the actual shipping container.
Below 10 million pounds, material is usually shipped using either a
returnable reusable container or a one-trip expendable container.
     Machinery used for packing bulk materials includes weighing and
bagging equipment and, for packing dry materials into drums and barrels,
filling and weighing equipment.
3.2.12  Emissions from Bagging and Bulk Loading Operations
     Bagging operations are a source of particulate emissions.  Dust-laden
air is emitted during the final stages of bag filling when air is forced
out of the bags.  An additional source of emissions is provided by con-
tainer agitation (vibrators) that is used to compact materials to increase
packaging efficiency.  Fine product materials that are not bagged for
shipment are either bulk loaded in tank trucks, drums, or enclosed rail-
road cars.  Product loading varies from plant to plant and differs for
the materials handled (i.e., uranium ores may require a sealed drum
                                 3-48

-------
while copper may be bulk loaded onto open railroad cars or trucks).   The
usual method of loading (unloading) is by gravity feed through plastic
sleeves.  Bulk loading of fine material is a source of emissions because
dust-laden air is forced out of the truck, drum, or railroad car during
product transfer.  Emissions would be affected by the same factors
discussed under conveyor transfer operations.  Emission rates are also
comparable.
3.2.13  Emission Factors for Related Industries
     Engineering estimates of uncontrolled emissions for crushed stone
or rock handling facilities have been made (EPA, 1979).  These factors,
included in Table 3-14, are suggestive of the range of emissions that
might be expected from the metallic minerals processing industries that
employ similar processes.
3.3  PROCESS EMISSIONS ALLOWED UNDER CURRENT STATE REGULATIONS
     Individual states currently use a variety of regulations and formulas
to determine allowable particulate emissions under the state implementation
plans (SIP).  Table 3-15 tabulates the various process weight equations
used by some states to determine allowable emissions from the metallic
mineral industry under the SIPs.  Table 3-15 shows that the allowable
emissions  (in pounds per hour) are an exponential function of the tons
of material processed through each unit process.
     In nonattainment areas stricter standards may be  applied.  The
State of Oregon, for example, will require an alumina  handling operation
now  under  construction to limit emissions to 0.05 g/DNm3  (0.02 gr/dscf).
     The major uncertainty in the application of SIP process weight
curves  is  the lack of a clear definition of  a "unit process," as applied
to the  metallic  mineral processing industry.  Because  processing is,  in
most cases, primarily a size-reduction operation, all  crushing, grinding,
and  screening operations could be grouped as one unit  process.  In
contrast,  the process weight curves could be applied separately to each
crushing,  grinding,, or screening operation.
     To calculate the difference in emissions between  the SIPs  and the
proposed NSPS, the model plants were  divided into several unit  processes.
For  the all-inclusive model plant  (such  as copper), six  unit processes
                                  3-49

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                 Table  3-15.   STATE  PROCESS WEIGHT EQUATIONS
 Maximum allowable emissions   (AE)
         in  pounds per  hour
                                      States
 AE =  55 p0'11  - 40
            0.16
AE = 17.31 p
AE = 11.78 p0-11

AE=0.76p°-42

AE = 24.8 p0-16

AE=4:ip0'67
- 18.14
Alabama  , Arizona, Florida,
Georgia  , Idaho, Illinois , Kansas
Louisiana, Michigan^ Montana,
Oklahoma, Tennessee , Virginia,
Wyoming

Alabama  , California, Colorado,
Kentucky, Maine, Minnesota,
Tennessee , Wisconsin, Wyoming0

Nevada9

Pennsylvania

Illinois'1

Georgi ae
 Process rate (p) in tons/hr and greater than 30 tons/hr, unless otherwise
 noted.

 For Alabama, a Class I source is located in a county with 50% or more of
 its population in urban areas, and where secondary national ambient air
 quality standards are exceeded.

GFor new sources.

 For existing sources with (p) greater than 450 tons/hr.
eFor existing sources.

 For Alabama, a Class II source is in a county not satisfying Class I
 conditions.

9Process weights (p) and emissions in kg/hr.

 For new sources with (p) greater than 450 tons/hr.
                                   3-51

-------
were defined as primary, secondary, and tertiary crushing, dryers,  fine
ore bin storage, and product loadout.  All screening and conveying
operations were combined with these unit processes.  The allowable
emissions for each unit process were then calculated on the basis of ore
processed by each unit process.  In cases where larger plants would
employ parallel crushing operations, the process weight curves were
applied to each crushing complex as a separate unit process on the basis
of the ore processed by that unit.  Because process weight curves vary
from state to state, selection of the most appropriate curve for each
mineral was based on the probable location of new facilities or major
ore reserves.  Table 3-16 presents the process weight equations initially
used to calculate emission reductions under the NSPS.  Table 3-17 shows
the emissions allowable under the State Implementation Plans,
     After the calculations described above were performed, and these
results were compared with"the expected performance of currently-used
emission control equipment, it became apparent that many facilities
could reduce emissions to a lower level than required by the SIP process
weight curves.  Thus, it was likely that the real impact of a proposed
new source performance standard (NSPS) would be overestimated.  Therefore,
a second set of calculations was performed, based on modeling the expected
performance of the most popular, currently-used emission control device
(a 6-inch pressure drop wet scrubber) (Sparks, 1978).  These calculations
will be described in greater detail  in Chapter 4.  These calculations
will also be used as a basis on which the cost-benefit analysis of the
regulatory alternatives will be performed (see Chapter 8).  The results
of the calculations are presented in Table 3-17 for plants projected
between now and 1985.
                                  3-52

-------
  Tab]e 3-1S,   HETALLIQ ^ERAL PROCESS  WEIGHT QjJRVES
      pljneral
Mranium
 Process y/ei0ht eq|ja£ionc

Aluminum

Copper
Gold
Iron
ILead/Zirjc

Molybdenum

Silver

AE =

AE s
AE =
AE =
AE =

AE =

AE =
0 11
55 pu-'H
0 11
§5 p'u
11.78 p0'
17.31 p°-
55 p0'11
A
17.31pQ'
n n
55 pg •'

, 4Q

s 41
^ - 18.14C
W
T' 4Q
ifi
4-P

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' ''\ '>..  '"" >? »--" I*1 '' •     , "T * *




                G

 AE  = 3.59 pQ^2



 AE  - 5,5 p-'^ '- 4Q^
         ratf  (p)  In tqns/hr, unless otherwise
               ''' '"       '      • .       ;  l  ' .' '•

         ratg  (p)  In kg/hr.

     25 ton/hour plant,


   r 75 ^on/hour plant,
                         3-53

-------
              Table 3-17.  BASELINE EMISSIONS BASED ON MODELLING
                          ON WET SCRUBBER PERFORMANCE

Metal
Aluminum
Copper
Gold
Iron
Lead/Zi nc
Molybdenum
Silver
Titanium/
Zirconium
Tungsten
Uranium
New and expanded
plant sizes
(tons ore/hr)
1 @ 150
1 @ 300
1 @ 150
1 @ 600 '
1 @ 75
1 @ 150
1 @ 1,200
1 @ 2,400
1 @ 300
1 @ 600
1 @ 300
2 @ 1,200
2 @ 50
1 @ 150
1 @ 300
1 @ 600
1 @ 25
2 @ 25
3 @ 75
Emissions under
modelled baseline
Mg/hr (tons/yr)
153
263
519
1,021
195
236
1,313
2,666
470
698
687
1,400
194
305
280
449
163
78
120
(168)
(289)
(570)
(1,124)
(215)
(260)
(1,444)
(2,932)
(517)
(767)
(756)
(1,540)
(213)
(336)
(308)
(493)
(180)
(86)
(132)
Emissions allowed
under SIP's
Mg/yr (tons/hr)
587
667
1,284
2,457
510
584
1,859
3,324
1,254
1,682
1,263
2,165
472
586
427
601
562
140
183
(645)
(733)
(1,413)
(2,703)
(561)
(642)
(2,045)
(3,657)
(1,380)
(1,850)
(1,390)
,(2,380)
(519)
(645)
(470)
(661)
(618)
(154)
(201)
a6-inch pressure drop wet scrubber.  Where multiple plants at a specific size"
 are projected, emissions are from an individual plant.
                                      3-54

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3.4  REFERENCES FOR CHAPTER 3

Allis-Chalmers.  1973a.  Model S H Ripl-Flo Inclined Vibrating Screens.
          Appleton, Wisconsin.  Bulletin 26 B 6151-05.  5 pp.

	.   1973b.  Standard Low-Head Vibrating Feeders.  Appleton, Wisconsin.
     Bulletin 26 B 9978-05.  3 pp.

	.   1975a.  Superior Gyratory Crushers.  Appleton, Wisconsin.
     Bulletin 17B-5477.  19 pp.

	.   1975b.  Vibrating Screens - Theory and Selection.  Appleton,
     Wisconsin.  Bulletin 26 M 5506.  27 pp.

	.   1977a.  A-l Jaw Crushers.  Appleton, Wisconsin.  Bulletin 17B-5883.
     11 pp.

	.   1977b.  Low-Head Horizontal Vibrating Screen.  Appleton, Wisconsin.
     Bulletin 26 B 6330-05.  5 pp.

Bixby-Zimmer Engineering Co., undated.  Our Business is Making Screens
     that Make You Money.  Galesburg, Illinois.  Bulletin 974.  39 pp.

Environmental Protection Agency (EPA).  1979.  Compilation of Air Pollution
     Emission Factors, Supplements 1-7.  AP-42.

Environmental Protection Agency (EPA).  1980.  Air  Pollutant Control
     Techniques for Crushed and Broken Stone Industry.  EPA-450/3-80-019.
     Research Triangle Park, North Carolina.

Perry,  J. H.  1963.  Chemical Engineer's Handbook.  McGraw-Hill Book
     Company, Inc.  New York, New York.  pp. 7-10,  8-3, 8-4, 8-10,
     8-14, 8-15, 8-19, 8-20.

Process Technology Corporation.  1978.  Kue-Ken Jaw Crushers.  Oakland,
     California.  Bulletin 802.  12 pp.

Rexnord, Inc.  1972.  Nordberg Heavy-Duty GP Screens.  Milwaukee, Wisconsin.
     Bulletin 389B.  8 pp.

	.   1975.  Symons Cone Crushers.  Milwaukee, Wisconsin.  Bulletin
     322G.  24 pp.

	.   1976a.  Nordberg Primary Gyratory Crushers.  Milwaukee, Wisconsin.
     Bulletin 408.  22 pp.

	.  I976b.  Nordberg Stationary Belt Conveyors.  Milwaukee, Wisconsin.
     Bulletin 409.  24 pp.

	.  1976c.  Nordberg Dynapactor Impact Crushers.  Milwaukee, Wisconsin.
     Bulletin 414.  11 pp.
                                 3-55

-------
Richards, R. H. and C. Locke.  1940.  Textbook of Ore Dressing.  McGraw-Hill
     Book Company, Inc.  New York, New York.  608 pp.

Skalos, C., Dravo Corporation.  1980.  Telephone conversation with E. Monnig,
     TRW, September 26.  Emission rates for metallic mineral operations.

Sraidth, F. L.  1978.  Mining Mills Basic Data.  Copenhagen, Denmark.
     17 pp.

Soderberg, H.  American Air Filter.  1980.  Telephone conversation with
     E. Monnig, TRW, August 7.  Emission rates for metallic mineral
     operations.

Sparks, L. E., 1978.  SR-52 Programmable Calculator Programs for Venturi
     Scrubbers and Electrostatic Precipitators.  EPA-600/7-78-026.
     U.S. Environmental Protection Agency.  Research Triangle Park,
     North Carolina.

Sweet, E., Reynolds Metals, Inc.  1980.  Telephone conversation with
     E. Monnig, TRW, October 1.  Emission rates for metallic mineral
     operations.

Universal Engineering Corp.  Undated.  Universal Jaw Crushers.  Cedar
     Rapids, Iowa.  Bulletin 8-100-117b.  8 pp.

U.S. Bureau of Mines.  1978.  Mineral Commodity Summaries.
     Washington, D. C.  200 pp.
                                 3-56

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                       4.   EMISSION CONTROL TECHNIQUES

4.1  INTRODUCTION
     This chapter discusses the basis for the selection of systems of
participate emission reduction for the metallic mineral processing
industries.  After considering the technical factors affecting the
application of various control systems, test data regarding the effective-
ness of particular systems are presented.  The implications of these
test data on the selection of control systems are then discussed.
     Fabric filter baghouses and wet scrubbers are commonly used
particulate emission control systems in the metallic mineral processing
industries.  Exhaust characteristics such as temperature, moisture
content, particle loading, and particle size distribution must be
considered when these systems are applied to a particular exhaust stream.
Baghouse and wet scrubber control technology can perform equally well on
many exhaust streams in the metallic mineral industries; however, there
may be factors that determine the selection of one type of system over
another.  In addition to the exhaust stream characteristic noted above,
these factors include the ease of disposal of collected particles
(whether wet or dry), the energy use of alternative systems, and the
cost of alternative systems.  These factors are discussed in this
chapter and in Chapters 7, 8, and 9.
     Two other types of control equipment, dry cyclones and dust
suppression systems with water/surfactant sprays, have been used on a
limited basis in the metallic mineral  industries.  Used by themselves,
neither dry cyclones nor wet suppression systems can provide emission
control as effective as baghouses or wet scrubbers.  However, either dry
cyclones or wet suppression may be used with good results to reduce the
load on these more efficient control devices.

-------
     Dry cyclones are frequently used as prefliters for more efficient
control devices.  Dryers and pneumatic conveyance systems that handle
fine material may require dry cyclones for efficient product recovery
before using an air pollution control device.  When dry cyclones are
used in this manner for product recovery, they are more properly
classified as mineral processing equipment rather than emission control
equipment.
     The emphasis on baghouse and wet scrubber control technology in
this document is a reflection of current industry practice.  Electrostatic
precipitators (ESP's) can also provide very effective particulate matter
removal.  Their use in the metallic mineral industries has been confined
to high temperature, high flow exhaust streams from calcining and
pelletizing operations.  As noted in Chapter 3, these process operations
are not covered in this document.  ESP's will be discussed briefly in
this chapter.
     The discussion in Chapter 3 of uncontrolled emission rates from
various processes indicates that a wide range of exhaust conditions are
expected in the metallic mineral industries.   A significant issue
considered throughout this document is the level of control baghouses
and wet scrubbers can achieve under worst-case inlet conditions.  The
design of control equipment to meet worst-case inlet conditions is
discussed extensively in this chapter.  The economic, energy, and
environmental impacts discussed in later chapters are also based on
worst-case inlet conditions and the design criteria and cost of
equipment necessary to meet worst-case inlet conditions.
     Emphasis on worst-case inlet conditions and the design of control
equipment to handle these conditions should not be interpreted as a
recommendation or a requirement that certain types of equipment would be
necessary to meet a specific emission level under all conditions found
in the metallic mineral industries.   The selection of control equipment
for an actual emissions source requires consideration of the char-
acteristics of only that source.  Rather, the discussions of worst-case
conditions are based on two premises.  First, if an emission level can
be demonstrated as achievable under worst-case conditions, then it is
                                 4-2

-------
achievable under all  conditions found in the industry.   Second,  if the
cost of achieving an emission level is based on the cost of control
equipment designed to meet that emission limit under worst-case  inlet
conditions, then the actual cost of control equipment designed to meet
the emission level under less than worst-case conditions should be less.
     In order to broaden the range of conditions considered for the
performance of the control equipment, test data for non-metallic mineral
processing facilities are also included in the data base discussed in
this chapter.  Data from the non-metallic industry further demonstrate
baghouse performance.  Data from the non-metallic mineral industries may
be appropriately transferred to the metallic mineral industries for
several reasons.  As noted in Chapter 3, much of the process equipment
of interest in this document is similar in the metallic and non-metallic
processing industries.  Because the ores from which metallic elements
are extracted are primarily non-metallic in character, the emissions
from metallic mineral processing operations are primarily non-metallic
mineral constituents.  Furthermore, the similarity of emissions from
metallic and non-metallic processes in key parameters such as particle
size distribution and mass loading provide additional evidence of
similarity between the two industries.  These measurements were
routinely made during the testing of both metallic and non-metallic
processing facilities and form the basis for extrapolating control
efficiency from one  industry, whether metallic or non-metallic, to
another.
     Finally, a comparison of non-metallic and metallic test data  indicates
that several sources tested  in the non-metallic mineral industries
provide more difficult control conditions than those tested in the
metallic mineral  industries.  These tests provided  information on  the
performance  of  baghouses  under rigorous conditions  and thus increase
understanding of  the range of circumstances  in which baghouses might  be
used.  These tests also help anticipate the  performance of baghouses
under  "worst-case" conditions  in  the metallic mineral industries.
     In addition  to  the adverse control conditions  provided by the
non-metallic industries,  an  additional  set  of control requirements was
projected.   When  the control of high-moisture emissions  is required
                                  4-3

-------
 under  conditions where condensation can occur, the effectiveness of
 baghouses may be reduced when the baghouse fabric is blinded.  Given the
 above  conditions, wet scrubbers might be the preferred control equipment.
 When such high moisture conditions were tested, control equipment
 particulate  loadings were low at these facilities and therefore did not
 indicate the entire range of conditions under which scrubbers might
 operate.  Because inlet loading might be higher under some
 circumstances, the performance of venturi scrubbers was mathematically
 modelled given higher uncontrolled emission rates than occurred at
 facilities with moisture problems.  These higher uncontrolled emission
 rates  occur  at facilities that are adequately controlled by baghouses
 where  moisture is not a problem, and the modelling exercises show that
 these  emissions could be controlled by wet scrubbers.  These modelling
 exercises are based on hypothetical conditions yet are illustrative of
 the performance of venturi scrubbers under worst-case conditions.  The
 results of this modelling are presented in Section 4.6.
     A final introductory note on the subject of particle size testing
 is appropriate because of the important role of particle size data in
 the prediction of control equipment efficiency.  The microscopic and
 individual analysis of particles emitted from the variety of mineral
 processing facilities under consideration here would reveal an array of
 shapes, sizes, and densities.  Individual consideration of the efficiency
 of control equipment on every member of this array is, of course,
 impractical.  Currently used aerodynamic sizing techniques reduce this
 infinite array of factors to one common denominator.   The typical cascade
 impactor sampling device groups particles by their aerodynamic behavior
 under a set  of known conditions.   These groups of particles are then
 assigned an  equivalent aerodynamic diameter (x) which is the diameter of
 a sphere of  unit density that would behave in the impactor in the same
manner as the actual group of particles.   These aerodynamic diameters
 become the basis for predicting the efficiency of control equipment and
make it possible to compare particles emitted from a wide range of
minerals.
                                 4-4

-------
4.2  FABRIC FILTERS
     Fabric filters are high efficiency collection devices frequently
used in the metallic mineral processing industries.  The greatest
variations in the design of baghouses arise from the methods of cleaning
the fabric filter, the choice of fabric for the filter, and the size of
the unit.
     The actual extraction of dust is accomplished by one of several
methods as shown in Figure 4-1.  The airstream enters the baghouse and
is pulled through fabric sleeves that are arranged throughout the apparatus.
In one design, external draw on the apparatus, pul1s the air to the
outside of these fabric sleeves which is a "clean area."  The dust
remains trapped in the weave of the sleeve forming a cake and the
cleansed air is exhausted to the atmosphere.  The reverse operation can
also be utilized; that is, particle-laden air can be pulled from the
outside to the inside of the bag and exits through either the top or the
bottom of the bag.  The dust then accumulates on the outside of the
sleeves.
     The accumulated dust forms a filter cake on the bags which must be
removed periodically if there is to be sufficient flow through the
system.  The system must be designed such that the dust is removed in
such a manner that it does not become re-entrained.  Major methods of
cleaning are shaking (rapping) and reversing air flow by air jets or
pulses.  Shaking consists of manually or automatically shaking the bag
hangers or rapping the side of the baghouse to shake the dust free into
a receiving hopper below.  Shaking typically occurs on a section of the
baghouse temporarily isolated from the gas stream.  After sufficient
time is allowed for the dust to settle the section is returned to service.
     A more complex cleaning method involves reversing air flow down the
tubes at such a rate that there is no net movement of air through the
bag.  As shown in Figure 4-2, this causes the bag to collapse and the
filter cake to break up.  A blast of air to the  inside of the bag then
removes the collected material.  This method of  cleaning usually requires
compartmentalizing the baghouse so that sections of the baghouse can be
isolated during the cleaning cycle.
                                 4-5

-------
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-------
     Another method is to pulse air through a perforated ring that
travels up and down the outside of each bag or sleeve.   Air jets  in the
ring force the bag to collapse and reopen, thus breaking the filter cake
apart.
     Baghouses that draw dirty air from outside the fabric sleeve to the
inside (thus collecting particles on the outside of the sleeve)  often
use a pulse jet cleaning system.  In this system a blast of compressed
air is forced down the inside of the fabric sleeve causing the sleeve to
expand slightly breaking off the accumulated cake.  This cleaning method
can be used without isolating the bags being cleaned; however, sufficient
space must be allowed between bags to avoid re-entraining dust.
     The frequency of cleaning can be determined by a timed cycle.
Alternatively, sensors can be installed which will start the cleaning
cycle when a specified pressure drop across the system occurs because of
the build up of the filter cake.
     Materials available for bag construction include cotton, Teflon,
Orion, nylon, Dacron, wool, Dynel, and others.  Temperature and other
operating parameters must be considered in selecting fabric material.
Host metallic mineral processes are at or near ambient conditions,
therefore, temperature is usually not a significant concern in the
industry.  The most popular material in terms of wear and performance
industry is Dacron felt.  Felted materials are used most frequently on
pulse jet units.  Other parameters considered in the selection of fabrics
and design of baghouses are the cleaning cycle frequency, cloth
resistances to corrosion, and ore moisture (Danielson, 1973, p.  110-116).
     The final major parameter considered is the air-to-cloth ratio or
filter ratio.  This parameter is defined as the ratio of air filtered
(in cubic meters or cubic feet per minute) to the area of the filtering
medium.  This ratio reduces to meters (or feet) per minute.  A filter
ratio that is too high results in excessive pressure drop, reduced
collection of particles, blinding, and rapid wear.  Too low a filter
ratio results in excessive expenditure for control equipment.  The
air-to-cloth ratio will vary with the type of baghouse.  Reverse air and
shaker baghouses typically require lower gross air-to-cloth ratios for
continuous operations than pulse jet baghouses in part due to the
                                 4-8

-------
necessity of closing off sections of the baghouse during reverse air or
shaker cleaning.  Typical ratios in the mineral processing industries
are 2:1 to 4:1 for reverse air and shaker systems and 5:1 to 9:1 for
pulse jet systems.  The correct ratio for a particular type of baghouse
depends on bag material and the particle size that is collected
(Danielson, 1973, p. 116; Usis, 1978).
4.3  PERFORMANCE DATA FOR FABRIC FILTER BAGHOUSES
4.3.1  Particulate Emission Data
     Particulate emissions were measured by EPA for 25 baghouses used to
control emissions from crushing, screening, drying, and conveying
operations at 13 mineral processing sites.  Table 4-1 presents, a summary
of baghouse types and filter ratios (air-to-cloth) of the baghouses
tested by EPA for which information was available.
     Considerable care was given to choosing facilities that represent
the range of conditions in the metallic mineral industry.  The most
adverse control conditions under which a facility could operate must be
considered in the design of a test.  For example, a facility is tested
only when it is operating at 80 percent of capacity or greater.
     The facilities chosen for testing were judged to be well designed,
maintained and operated.  Despite the effort made to coordinate testing
with industry schedules and patterns and the efforts of industry repre-
sentatives to ensure representative conditions, occasional equipment
breakdown or other unanticipated malfunctions can hamper testing or
result in completely nonrepresentative conditions.  This may result in
test data that are also nonrepresentative.  Such cases were few in the
testing program undertaken for the metallic mineral processing industry
and provided the only conditions under which data were disregarded.
     In most cases a single piece of control equipment collected emissions
from several pieces of process equipment.  In these cases attempts were
made to measure the emission characteristics both before as well as
after the wet scrubber.  In the discussion below, the use of the term
"combined inlet duct" in reference to inlet characteristics refers to
actual measurements taken at a duct at a point beyond the junction of
individual process ducts.  In some cases it was not possible to measure
                                 4-9

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a combined inlet duct; instead, a weighted average of individual  inlet
emission concentrations is given below to compare inlet and outlet
concentrations.  Figure 4-3 presents inlet loadings to the baghouses
tested.  These concentrations represent the particle levels at the inlet
of the tested baghouses.   Figures 4-4 and 4-5 present emission levels
after baghouse control.
     Particle size distribution data are reported below for most inlet
and outlet streams.  Typically, three tests were run for the inlet
particle size distributions.  Only one test was made of outlet particle
size distribution because outlet size is not significant for the
prediction of control equipment efficiency.  The inlet particle size
data are presented as the average of the runs unless the data varied
significantly from run to run.
     Plant A processes copper ore mined from low grade deposits
(0.5 percent copper) into concentrate.  This plant used a baghouse (Al)
to control emissions from a rail car loading operation that handled
copper ore concentrate.  Use of baghouses under these conditions is
fairly common because the valuable product captured by the baghouse can
be returned directly to the operation.  A weighted average of the truck
loadout hood and the conveyor exhaust gave a calculated combined inlet
concentration of 0.71 g/DNm3 (0.31 gr/dscf).  The baghouse outlet con-
centration averaged 0.03 g/DNm3 (0.013 gr/dscf) as shown in Figure 4-4.
Twenty percent of the inlet particles at both truck loadout hood and
conveyor belt exhaust were smaller than 4 microns.
     Plant F processes iron ore mined from an open pit operation.  This
plant was tested on two occasions, once in 1973 and again in 1978 after
the wet scrubbers had been replaced by baghouses.  The results of 1973
test will be reported in Section 4.5.
     Baghouse Fl controlled the emissions from a secondary and tertiary
crushing operation and associated screens.  The outlet concentration
averaged 0.008 g/DNm3 (0.003 gr/dscf) and ranged from 0.007 to
0.009 g/DNm3 (0.003 to 0.004 gr/dscf).  No inlet measurements or
particle size distributions were taken.
     Baghouse F2 at Plant F controlled emissions from the system that
conveyed ore from the fine crushers to the concentrator.  The inlet con-
centration averaged 3.0 g/DNm3 (1.31 gr/dscf) and the outlet average

                                 4-12

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            Figure 4-3.  Inlet loadings to baghouses .in the metallic and
                         non-metallic minerals processing industries.

                                        4-13

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           01  02  03 04  Kl K2      LI  L2 Ml  M2 Nl  N2 01  PI ?2  Ql Q2



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       Figure 4-5.   Participate emissions  from baghouses at  non-metallic

                     minerals processing operations.

                                                                                 1
                                       4-15

-------
 0.009 g/DNm  (0.004 gr/dscf).   No particle size data were taken at this
 facility.
      Baghouse F3 controlled emissions from an ore car dump.   The outlet
 concentration averaged 0.007 g/DNm3 (0.003 gr/dscf).   No inlet  measurements
 or particle size distributions were taken.
      Plant G processes copper ore from an open pit mine.   Baghouse Gl
 controls emissions from a primary crusher complex including  two grizzly
 screens, the primary crusher hood,  and ore bins.   As  shown in Figure 4-3,
 the combined inlet duct concentration averaged 5.43 g/DNm3 (2.37 gr/dscf)
 and the outlet averaged 0.013  g/DNm3 (0.006 gr/dscf).   Particle sizes of
 the combined inlet flow were relatively large.   Ninety-five  percent of
 the inlet  particles were greater  than 8 microns whereas  25 percent of
 the outlet particles were greater than 8 microns,  as  shown in Figure
 4-6.  The  particle size distributions taken at the grizzly screen  duct
 and the primary  crusher hood duct were similar to  the  combined  inlet
 duct.
      Baghouse  G2 controlled  emissions from  two truck dump  stations  from
 which ore  was  fed to the primary  crusher.   The combined  inlet concentra-
 tions averaged 0.304 g/DNm  (0.133  gr/dscf)  while  the  outlet  averaged
 0.041 g/DNm  (0.018 gr/dscf).  As shown  in  Figure  4-7, 50  percent of the
 inlet particles  were less  than 4  microns while  20  percent  of  the outlet
 particle size  distribution was below that level.
      Plant H processed  imported bauxite  into alumina.  One pulse jet
 baghouse controlling emissions from  an ore bin  complex was tested.  The
 control equipment  configuration prevented sampling  of the  inlet duct.
                                                    o
The outlet from  these ore bins averaged 0.007 g/DNm  (0.003 gr/dscf) and
 ranged  from 0.007  to  0.009 g/DNm3 (0-003 to  0.004 gr/dscf).
      Plant I processed gold ore from  an underground mining operation.
The baghouse at  the  milling operation controlled emissions from the
primary, secondary,  and tertiary crushers, an ore storage  inlet, and
associated conveyor transfer operations.  This baghouse had a design
air-to-cloth ratio of 9.1:1 and operated with a pulse jet cleaning
system.
     During the testing of this baghouse, ore from 1500-1800  meters
(5000-6000 feet) underground was being processed.  This ore was
                                 4-16

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characterized by high levels of unbound water (4 to 5 percent) and warm
temperatures (25 to 30°C (80° to 90°F)) due to the depths from which it
was extracted.   Because milling took place at the surface where the
winter temperature was 0 to 7°C (30 to 45°F) condensation of moisture in
the inlet ducts of the baghouse was very evident.  The high moisture
emissions combined with the relatively high air-to-cloth ratio caused
blinding of the fabric filters rendering the pulse jet cleaning system
ineffective.  As a consequence, the pressure drop at the baghouse rose
beyond design levels.  To circumvent this problem, the filter bags were
cleaned by manually air-lancing them before each test.  The pressure
drop at the baghouse was monitored closely during the tests.  The
implications of high moisture on the choice and performance of control
equipment will be further discussed in Section 4.8.
     The duct configuration of the baghouse prevented measurement of the
combined inlet concentration.  The weighted average of the crusher
inlet, the conveyor transfer inlet, and the ore storage reclaim inlet
resulted in a concentration of 0.39 g/DNm  (0.17 gr/dscf).  The outlet
concentration averaged 0.015 g/DNm3 (0.007 gr/dscf).  The particle size
distribution at all three inlet ducts were similar.  As shown in
Figure 4-8, 30 to 40 percent of the particles were less than 10 microns
in diameter.
     Plant J processed limestone for the manufacturing of cement.
Baghouse Jl controlled emissions from a primary crusher.  As shown in
Figure 4-5, the outlet concentration averaged 0.013 g/DNm  (0.006 gr/dscf).
The inlet concentration was not measured; however, particle size at the
inlet to the baghouse was measured.  As shown in Figure 4-9, 98 percent
of the particles were greater than 6 microns.
     Baghouse J2 controlled emissions from the primary crusher screen.
                                                                     o
As shown in Figure 4-5, the outlet concentration averaged 0.005 g/DNm
(0.002 gr/dscf).  Particle size at the primary screen was similar to
that at the primary crusher, as shown in Figure 4-9.  Baghouses J3 and
J4 controlled emissions from a primary crusher transfer point and a
secondary screen/crusher, respectively.  Outlet concentrations averaged
0.004 and 0.002 g/DNm3 (0.002 and 0.001 gr/dscf) at these two baghouses,
respectively.  No inlet measurements were taken.
                                 4-19

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     Plant K produces crushed limestone and agricultural  lime,.   Two
baghouses were tested - one controlling emissions from a primary impact
crusher, and the second controlling emissions from the secondary crusher
complex including a scalping screen, a secondary cone crusher,  a hammer
mill, the top of both finishing screens, five product bins, and six
conveyor transfer points.  The inlet concentration at Baghouse  Kl averaged
14.42 g/DNm3 (6.30 gr/dscf) (Figure 4-3) while the outlet averaged
0.016 g/DNm3 (0.007 gr/dscf) (Figure 4-5).  The outlet of the secondary
crusher complex (Baghouse K2) averaged 0.009 g/DNm3 (0.004 gr/dscf).   No
inlet measurements were taken at Baghouse K2.
     Plant L produced various sized aggregates and crushed stone from
limestone.  Two baghouses were tested at this plant.   Baghouse  LI controlled
emissions from a primary crusher, a scalping screen and a hammer mill.
Baghouse L2 controlled emissions from two sizing screens and two
conveyor transfer points.
     A weighted average of the concentration in the duct from the primary
crusher and the duct from the scalping screen and hammermill was calcu-
lated to be 2.5 g/DNm3 (1.1 gr/dscf).  The outlet of Baghouse LI averaged
0.005 g/DNm3 (0.002 gr/dscf).  The outlet concentration of Baghouse L2
was again very low and averaged 0.005 g/DNm3 (0.002 gr/dscf) (see
Figure 4-5).  No particle size testing was performed at either baghouse.
     Plant M produced road base stone and various grades of.bituminous
aggregate from traprock.  Traprock is a generic term for various dark
colored, fine grained igneous rocks composed of ferromagnesian minerals
and basic feldspars with little or no quartz.  Of the two baghouses
tested at this plant, Ml collected emissions from the secondary and
tertiary crushers and associated screens and M2 collected emissions from
the final sizing screens and associated transfer and discharge points.
Baghouse 1 averaged 0.02 g/DNm3 (0.009 gr/dscf) at its outlet while
Baghouse 2 averaged 0.007 g/DNm3 (0.003 gr/dscf).  No measurements of
particle size or concentration were taken at the inlet to these baghouses.
     Plant N processes traprock into a variety of crushed stone aggregate
products ranging from road base stone, concrete aggregate and bituminous
aggregate.  Baghouse Nl at this plant controlled emissions  from four
tertiary crushers and associated sizing screens and conveyor transfer
                                 4-22

-------
points.   Baghouses N2 controlled emissions from five finishing screens
and eight conveyor transfer points.   The outlets from Baghouse Nl and
Baghouse N2 both averaged 0.030 g/DNm3 (0.013 gr/dscf).   No inlet
measurements were taken.
     Plant 0 is a feldspar crushing, grinding, and milling operation.
The baghouse tested at this operation controlled emissions from a pebble
mill (ball mill), bucket elevator, two conveyor transfer points, and a
product loadout station.  Two inlet ducts, which together represented
the total flow to this baghouse, were tested.  A weighted average of the
concentrations at these ducts gave a total inlet concentration of
13.85 g/DNm3 (6.05 gr/dscf).   The outlet from this baghouse averaged
0.011 g/DNm3 (0.005 gr/dscf).  The particle size distributions at the
two inlet ducts were similar.  A weighted average of the particle size
distribution was taken and the median particle size was 25 microns as
shown in Figure 4-10.
     Plant P processed kaolin for use in the stoneware industry.  Bag-
house PI at this plant controlled emissions from a Raymond impact mill.
The inlet concentration measured 10.36 g/DNm3 (4.53 gr/dscf) while the
outlet averaged 0.037 g/DNm  (0.016 gr/dscf).  The particle size distri-
bution of emissions from this impact mill represents a relatively difficult
control  condition.  As shown in Figure 4-11, 50 percent of the particles
were less than 3.8 microns and 10 percent were less than 1.7 microns.
     Baghouse P2 controlled emissions from a roller mill.  The inlet
concentration measured 4.03 g/DNm3 (1.76 gr/dscf) while the outlet
averaged 0.016 g/DNm3 (0.007 gr/dscf).  The particle sizes at the duct
from this process were similar to those for Baghouse PI.  As shown in
Figure 4-12, 50 percent of the particles were less than 3.5 microns and
10 percent were less than 1.5 microns.
     Plant Q processed fuller's earth from attapulgite-type clay deposits.
Baghouse Ql controlled emissions from a roller mill.  The inlet
concentration to this baghouse was 11.99 g/DNm3 (5.24 gr/dscf) while the
outlet averaged 0.005 g/DNm3 (0.002 gr/dscf).  Particle size data taken
at the inlet to this baghouse indicate a normal distribution (in the
statistical sense) rather than the more typically seen skewed
                                 4-23

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              4-26

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distribution.   As shown in Figure 4-13, the particles at this test point
were relatively small with 57 percent of the particles between 3.5 and
8 microns in diameter.
     The emissions ducted to Baghouse Q2 presented the most difficult
control conditions encountered at any metallic or non-metallic facility
due to extremely small sized particles coupled with a relatively high
uncontrolled emission rate.  This baghouse controlled emissions from a
fluid energy mill that reduces particles to 1 to 20 microns in size (see
Section 3.2.1.5 for a more complete description).  Simultaneously the
mill pneumatically classifies material by size by'allowing the smaller
particles to escape with the vent exhaust.  After the bulk of the sized
material is removed from the airstream, exhaust from the fluid energy
mill at Plant Q is vented to a baghouse.  The particle size distribution
taken at the inlet to the baghouse reflects the size reduction of the
mineral in the fluid energy mill.  Fifty percent of the particles were
less than 1.5 microns and 20 percent of the particles were less than
0.7 microns, as shown in Figure 4-14.  The inlet concentration measured
2.38 g/D.Nm3 (1.04 gr/dscf) while the outlet averaged a very low level of
0.007 g/DNm3 (0.003 gr/dscf).
4.3.2  Visible Emission Data
     Visible emission observations were also made during the emission
tests described above.  The opacity of the exhaust from each of the
baghouses was observed in accordance with EPA Method 9 procedures
(Appendix A 40 CFR Part 60).  Method 9 measures emissions in terms of
percent opacity ranging from 0 percent, representing no interference
with transmission of light, to 100 percent, representing complete inter-
ference with light transmission.  Readings are taken at 15 second intervals
and averaged over 6-minute periods.
     As shown in Table 4-2, 21 of 24 baghouses showed zero emissions
during all observation periods.  The highest 6-minute average recorded
at Plant K was 1 percent opacity.  The highest 6-minute average for
Baghouse 1 at Plant G was 1-percent opacity and for Baghouse 2, the
highest reading was 6-percent opacity.
                                 4-27

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distribution.   As shown in Figure 4-13, the particles at this test point
were relatively small with 57 percent of the particles between 3.5 and
8 microns in diameter.
     The emissions ducted to Baghouse Q2 presented the most difficult
control conditions encountered at any metallic or non-metallic facility
due to extremely small sized particles coupled with a relatively high
uncontrolled emission rate.  .This baghouse controlled emissions from a
fluid energy mill that reduces particles to 1 to 20 microns in size (see
Section 3.2.1.5 for a more complete description).  Simultaneously the
mill pneumatically classifies material by size by allowing the smaller
particles to escape with the vent exhaust.  After the bulk of the sized
material is removed from the airstream, exhaust from the fluid energy
mill at Plant Q is vented to a baghouse.  The particle size distribution
taken at the inlet to the baghouse reflects the size reduction of the
mineral in the fluid energy mill.  Fifty percent of the particles were
less than 1.5 microns and 20 percent of the particles were less than
0.7 microns, as shown in Figure 4-14.  The inlet concentration measured
2.38 g/DNm3 (1.04 gr/dscf) while the outlet averaged a very low level of
0.007 g/DNm3 (0.003 gr/dscf).
4.3.2  Visible Emission Data
     Visible emission observations were also made during the emission
tests described above.  The opacity of the exhaust from each of the
baghouses was observed in accordance with EPA Method 9 procedures
(Appendix A 40 CFR Part 60).  Method 9 measures emissions in terms of
percent opacity ranging from 0 percent, representing no interference
with transmission of light, to 100 percent, representing complete inter-
ference with light transmission.  Readings are taken at 15 second intervals
and averaged over 6-minute periods.
     As shown in Table 4-2, 21 of 24 baghouses showed zero emissions
during all observation periods.  The highest 6-minute average recorded
at Plant K was 1 percent opacity.  The highest 6-minute average for
Baghouse 1 at Plant G was 1-percent opacity and for Baghouse 2, the
highest reading was 6-percent opacity.
                                 4-27

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            4-29

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Table 4-2.  OPACITY MEASUREMENTS FROM
       BAGHOUSE EXHAUST STACKS
Mean
opacity
Baghouse Processes controlled (percent)
Al


Fl


F2
F3
Gl


G2
HI
11


Jl
J2
J3
J4
Kl
K2
LI
L2

Ml

M2
Nl
• N2

01


PI
P2
Ql
Q2
Product loading including truck
dump hopper, and rail car
loading.
Secondary and tertiary crushing
operations and associated
screens. }
Conveyor transfer points.
Ore car dump.
Primary crusher complex includ-
ing grizzly screens, primary
crusher hood, and ore bins.
Truck dump hopper.
Ore storage bin.
Primary, secondary, and tertiary
crushers, ore storage, and
conveyor transfer points.
Primary crusher.
Primary crusher screen.
Primary crusher transfer point.
Secondary crusher and screen.
Primary crusher.
Secondary crusher complex.
Primary crusher and hammer mill.
Screens and conveyor transfer
points
Secondary and tertiary crushers
and screens.
Screens and transfer points.
Tertiary crushers and screens.
Screens and conveyor transfer
points.
Pebble mill, bucket elevator,
transfer points, and product
loadout.
Impact mill.
Roller mill.
Roller mill.
Fluid energy mill.
0


0


0
0
0


1
0
0


0
0
0
0
0
0
0
0

0

0
0
0

0


0
0
0
0
Highest
6 minute
average
opacity
(percent)
0


0


0
0
1


6
0
0


0
0
0
0
1
1
0
0

0

0
0
0

0


0
0
0
0
Lowest
6 minute
average
opacity
(percent)
0


0


0
0
0


0
0
0


0
0
0
0
0
0
0
0

0

0
0
0

0


0
0
0
0'
                  4-30

-------
     Data on fugitive emissions at hoods, pickup points and other capture
systems used in conjunction with baghouses are presented in Section 4.8.
4.4  SCRUBBERS
     Information gathered from industry under authority of Section 114
of the Clean Air Act indicates that wet scrubbers with pressure drops of
1.2 to 2.0 kPa (5- to 8-inches water gauge (w.g.)) are the most commonly
used emission control devices in the metallic mineral processing industry.
The numerous types of wet scrubbers cannot be conveniently represented
by one design; however, all wet scrubbers follow the same principle of
bringing contaminated air into contact with a liquid and subsequently
separating the particle-contaminated liquid from the airstream.  The
actual mechanism for effecting this contact varies with design as
discussed below.
     The most important parameters to be considered in the application
of wet scrubbers include the energy imparted in the liquid-gas mixing
process (measured as pressure drop), the amount of scrubber water used
per volume of gas (liquid-to-gas ratio), inlet particle size and concen-
tration, and the emission limits to be achieved.  Generally, higher
pressure drops across a wet scrubber increase the likelihood of contact
between the scrubbing liquid and individual particles.  Higher removal
efficiencies thus require higher energy input.
     The difficulty of removing particulate material increases markedly
with decreased particle size.  As particle size decreases, the surface
area-to-mass ratio increases so that surface properties can dominate
over mass properties.  As this happens, higher velocities and more acute
changes in direction are required to separate the particle from the gas
stream.  A typical 1.5 kPa (6 inch) wet scrubber exhibits removal
efficiencies of 80 to 99 percent for particles in a range of 1 to
10 microns in diameter.  High-energy wet scrubbers with pressure drops
of 7.5 kPa (30 inches) can achieve efficiencies of 99.0 to 99.9 percent
for particles in the 1 to 10 micron range and 95 to 99 percent for
particles from 0.2 to 1 micron (Theodore and Buonicore, 1978, p. 5-33).
     Given a scrubber collection efficiency reflecting a pressure drop,
liquid-to-gas ratio, and particle size distribution, the emission level
                                 4-31

-------
will be a function of the inlet concentration.  Over normal operating
ranges emission levels are a relatively constant percentage of inlet
1oadi ng.
     Several wet scrubber designs are popular in the metallic mineral
industry.  One common type is the dynamic or mechanically aided scrubber,
as shown in Figure 4-15.  In this type of collector the scrubber liquid
is introduced just prior to the fan.  The fan acts as a propeller of the
gas stream, a mixer for the gas and liquid streams, .and an impingment
surface for particles and contaminated liquid.  Water is typically added
at a rate of 75 to 150 liters per 1000 cubic meters (0.5 to 1 gallon per
1000 cubic feet) of gas.
     Several manufacturers offer improvements on the dynamic scrubber
design by adding preconditioning sections to the scrubber.  These
preconditioning sections utilize cyclonic flows and liquid additions to
provide an initial mixing of the scrubber liquid and the gas stream.
     High energy scrubbers are most commonly designed as venturi scrubbers.
High collection efficiency is achieved by increasing the relative velocity
of the scrubber liquid and the gas stream, thereby increasing the particle
droplet impaction rate.   In a venturi scrubber the gas velocity is
increased to 4,000 to 8,000 meters per minute (219 to 437 feet per
second) through a constricting throat (see Figure 4-16).  The scrubbing
liquid is introduced slightly ahead of the throat and is atomized by the
high velocity gas.  Water is typically added at a rate of 800 to
1340 liters per 1000 cubic meters (6 to 10 gallons per 1,000 cubic feet)
of gas.  The energy used by a venturi scrubber is primarily a .function
of the pressure drop across the venturi throat.   Pressure drops of 1.5
to 14.9 kPa (6 to 60 inches) are possible.
     After the thorough mixing of gas and liquid, the particulate-con-
taminated droplets are separated from the gas stream.   This separation
typically occurs in a separator adjoining the venturi  throat as shown in
Figure 4-16.  The increased size and inertia of the droplet-particle
combination forces it to the side of the cyclone and the clean air exits
through the cyclone top.
                                 4-32

-------
                                                 Water  Spray
        Vanes
Exhaust
                                                                Laden
                                                        .:*:•"  A1r
  4-15.  Generalized depiction of a dynamic or mechanically-aided
         wet scrubber.
                                 4-33

-------
                    Dirty Gas Inlet
  Scrubbing ..
Liquid Inlet
         VentuH
         Throat
         Flooded
          Elbow
                            Drain

                     Wet Approach
                   Venturl  Scrubber
                                               Clean Gas Outlet

                                                   O
                                                 Slurry Outlet
        Figure  4-16.   Generalized  depiction of a venturi scrubber.
                                      4-34

-------
     Wet scrubbers used in the metallic mineral industries are most
often constructed of carbon steel with the option of plastic or resinous
coating.  Under corrosive or acidic conditions the use of stainless
steel and the buffering of scrubber liquids are options.
4.5  PERFORMANCE DATA FOR WET SCRUBBERS
4.5.1  Particulate Emission Data
     Particulate emission measurements were conducted by EPA on 13 wet
scrubbers used to control emissions from crushing, screening, drying,
and conveying operations at 7 metallic mineral processing sites.   As
with baghouses, one wet scrubber often controls the emissions from
several process steps.  The term "combined inlet duct" will be used in
the same context described in Section 4.3 (Performance Data for Bag-
houses).  Figures 4-17 and 4-18 present the inlet data for the wet
scrubbers tested.
     As noted in Section 4-4, 1.5- to 2.0-kPa (6- to 8-inch) pressure drop
wet scrubbers are widely used in the industry.  The test data reported
below reflect the current industry practice.  These test data demonstrate
two general sets of conditions in the industry.  First there is a midrange
of conditions at a large number of plants that can be effectively con-
trolled with equipment similar to that currently used in the industry.
On the other hand, the inlet test data presented in this section and in
the section on baghouse performance indicate the possibility that worse
conditions may occur that are not suited to control techniques currently
used in the industry.  Although baghouses are well suited to small
particle size, high concentration emissions, high moisture conditions
may preclude their use in some cases.  High energy wet scrubbers may be
better suited to the worst cases which involve a combination of relatively
small particle size, high emission levels, and high moisture conditions.
Because few wet scrubbers above 2.5-kPa (10-inch) pressure drop are
available for testing in this industry, Section 4.6 is devoted to mathe-
matical modelling of the performance of high energy wet scrubbers.
     Plant A processed copper ore mined from low grade ore deposits
(0.5 percent copper) from an open pit mine in Arizona.  Two wet scrubbers
were tested at this operation.  Wet scrubber Al (1.5-kPa (67Inch) pressure
                                 4-35

-------
0.3 r
0.2
i
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              Al   A2   61
                                 KEY

                                 Average



                                 Test Points
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                       C4    Dl
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                             FACILITY
                          36.8
                                                        32.2
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                                   o
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 Figure 4-18.  Inlet loadings to-wet scrubbers. C4 through HI In

               the metallic minerals processing Industry.(note

               scale change-from Figure 4-23).
                             4-37

-------
drop) controlled emissions from the primary crusher surge bin and
associated conveyor transfer points.  As shown in Figure 4-17, the
combined inlet duct concentration averaged 0.501 grams per dry normal
cubic meter (g/DNm3) (0.219 grains per dry standard cubic foot (gr/dscf))
and outlet concentration averaged 0.025 g/DNm  (0.011 gr/dscf) as shown
in Figure 4-19.  Figure 4-20 presents the average particle size
distribution for the combined inlet duct and the outlet duct.
Approximately 60 percent of both the inlet and outlet particles were
greater than 7 microns though the outlet showed a higher percentage of
submicron particles.  By comparison with the combined inlet, the particle
size distribution of primary crusher surge bin showed 97 percent of the
particles greater than 7 microns.   The conveyer inlet duct was closer
to the combined inlet distribution with 65 percent of the particles
greater than 7 microns. A third inlet duct to the total scrubber inlet
was not tested for particle size distribution.
     Wet scrubber A2 (1.5-kPa (6-inch) pressure drop) at Plant A controlled
emissions from a secondary crushing operation and an ore reclaim operation.
Reclaiming refers to the process of withdrawing ore from a storage area
and conveying it to a processing operation.  As shown in Figure 4-17,
the combined inlet concentration averaged 0.622 g/DNm  (0.272 gr/dscf)
and as shown in Figure 4-19, the outlet concentration averaged
0.041 g/DNm3 (0.018 gr/dscf).  Figure 4-21 presents the average particle
size distribution for both the combined inlet and the outlet particulate
emissions.  Approximately 70 percent of the combined inlet particles
were greater than 7 microns while 85 percent of the outlet particles
were greater than 7 microns.  Theoretically the outlet particles should
show a smaller size distribution because the wet scrubber preferentially
collects larger particles.  The larger outlet particles may represent
the agglomeration of smaller particles that occurs under the high
moisture conditions following the scrubber.
     Based on an average of 3 runs as shown in Figure 4-21, 78 percent
of the particles from the secondary crusher alone were greater than
7 microns compared with 95 percent from the primary crusher.  In
principle, one might expect smaller particle sizes from finer crushing
                                 4-38

-------
0.15
0.10
0.05
 0.02
               KEY
               Average

               Ttst
                                                                     0.23'
                                                                         Cl
        Al  A2  Bl      B2  S3   Cl   C2  C3  C4  01

                         FACILITY
II  tl   HI
  Figure 4-19.   Particulate emissions  from low energy wet scrubbers
                 at metallic minerals processing operations
                 (see Section  4.6 for high energy wet scrubber
                 performance).
                                  4-39

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operations, although in this case the difference between primary and
secondary crushing operations may be an artifact of the data.   In the
case of the secondary crusher 2 runs showed 93 percent of the  particles
greater than 7 microns, and the third run showed 50 percent greater than
7 microns.
     Plant B processes molybdenum from ore mined from an underground
deposit in Colorado.  Three wet scrubbers were tested at this  plant.
All three scrubbers operated with a 1.5- to 2.0-kPa (6- to 8-inch) pressure
drop.
     Scrubber Bl controls emissions from a primary crusher pit, apron
feeder, and a conveyor transfer point.  In addition to controlling
emissions from the primary crusher by ducting emissions through a wet
scrubber, Plant B also uses a wet suppression spray system at  the crusher
pit.
     Measurements of the combined inlet duct at this scrubber  were not
possible.  Therefore, a weighted average of the concentrations measured
at the crusher pit inlet duct and the combined apron feeder duct and
conveyor duct was taken to determine the total inlet concentration. As
shown in Figure 4-17, the combined inlet concentration, as calculated,
averaged 0.302 g/DNm3 (0.132 gr/dscf).  The outlet concentrations were
low with an average of 0.012 g/DNm3 (0.005 gr/dscf) as shown in
Figure 4-19.  Between 33 and 42 percent of the particles from the transfer
point and the crusher pit were less than 8 microns as shown in
Figure 4-22.  The scrubber exhaust outlet showed 75 percent of the
particles to be less than 8 microns (Figure 4-23).
     Wet scrubber B2 controlled emissions from a pebble milling operation.
Emissions were collected from the screening operation before the mill
and a bucket elevator transfer point.  The combined inlet concentration
averaged 0.137 g/DNm3 (0.060 gr/dscf) while the outlet concentration
averaged 0.016 g/DNm3 (0.007 gr/dscf) as shown in Figures 4-17 and 4-19
respectively.  Approximately 30 percent of the combined irtVet particles
were less than 8 microns while 83 percent of the outlet particles were
less than 8 microns as shown in Figure 4-24.  Approximately 50 percent
of the particles from bucket elevator duct and 50 percent of the particles
from the mill screen duct were less than 8 microns.
                                 4-42

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              4-45

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     The wet scrubber B3 controlled emissions from ore concentrate
dryers.  As shown in Figure 4-17, the combined inlet from the dryers
averaged 0.51 g/DNm3 (0.224 gr/dscf) while the scrubber outlet averaged
0.020 g/DNm3 (0.009 gr/dscf) as shown in Figure 4-19.   Particle sizes
were significantly smaller than with the other operations.   As shown in
Figure 4-25, 90 percent of the particles were less than 8 microns and
45 percent of the particles were less than 2 microns.   The outlet particle
size distribution was similar with 96 percent of the particles less than
8 microns.
     Plant C processes uranium from ore deposits extracted from ar)
underground mine in Wyoming.  Four scrubbers were tested at Plant C.
Wet scrubber Cl (8-inch pressure drop) controlled emissions from a
primary crusher complex including the crusher and vibrating grizzly
exhaust duct and the conveyor transfer point exhaust system.  The con-
tribution of a third duct system exhausting a second set of conveyors
was not tested directly.
     The inlet concentrations were very low from this operation; in
fact, the uncontrolled emission rates at this plant compare favorably
with the controlled emission rates at other plants tested.   As shown in
                                                              3
Figure 4-17, combined inlet concentration averaged 0.021 g/DNm
(0.009 gr/dscf) while the outlet averaged 0.008 g/DNm  (0.004 gr/dscf)
as shown in Figure 4-19.
     Wet scrubber C2 (1.5-kPa (6-inch) pressure drop) controls the
emissions from the fine ore bins and associated transfer points.
                                                                       3
Uncontrolled inlet emissions were again very low, averaging 0.010 g/DNm
(0.004 gr/dscf) as shown in Figure 4-17.  The outlet concentration
averaged 0.005 g/DNm3 (0.002 gr/dscf) (see Figure 4-19).
     The particle size distributions of the combined inlets to both Cl
and C2 indicated a high percentage of submicron particles as shown  in
Figure 4-26.  Extrapolation of these distributions to conditions with
higher uncontrolled emission rates would not be reliable because of the
bias in the very low uncontrolled emission rates.  By comparison the
uncontrolled emissions from the dryer (see C4 below) had a median particle
                                                   o
size of 6 microns and a concentration of 5.15 g/DNm  (2.25 gr/dscf).
                                 4-46

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     Wet scrubbers C3 and C4 control emissions from operations that
occur after the beneficiation of uranium ore.   As discussed in Chapter 3,
the environmental, energy, and economic impacts of the control of these
operations will not be covered in Chapters 6,  7, and 8 of this document.
Because the radioactive composition of these emissions should not affect
the control of total particulate emissions, test results from these
scrubbers are included because of their relevance to the control of
emissions from drying and product loadout operations.
     Wet scrubber C3 controlled emissions from the yellowcake packing
area.  The outlet concentration averaged 0.010 g/DNm3 (0.004 gr/dscf),
as shown in Figure 4-19.  Uncontrolled emissions from this packaging
process were not tested.  The outle't duct from scrubber C3 is joined
with the inlet duct to wet scrubber C4.  The emissions from the packaging
operation are thus treated by two scrubbers in series.
     Wet scrubber C4 (1.5-kPa (6-inch) pressure drop) also controls
emissions from a yellowcake drying operation.   Uncontrolled emissions
from this drying process were considerably higher than at the other
facilities at Plant C and averaged 5.157 g/DNm3 (2.254 gr/dscf).  The
total inlet concentration to scrubber C4 was taken as a weighted average
of the dryer duct and the packaging operation duct.  This inlet concen-
tration averaged 2.06 g/DNm3 (0.90 gr/dscf) while the outlet averaged
0.156 g/DNm3 (0.068 gr/dscf), as shown in Figure 4-18 and 4-19 respectively.
Figure 4-26 shows an average of 18 percent of the particles from the
dryer inlet to the wet scrubber are below 2 microns and 40 percent are
less than 5 microns.  Seventy percent of the outlet particles were less
than five microns.  The particle size distribution found at the dryer
exhaust is more indicative of the range of particle sizes that would
occur if this material was processed under drier conditions with
consequently higher uncontrolled emission rates.
     Plant D processes vanadium from ore and slag.  Vanadium ores are
extracted from an open pit operation.  Wet scrubber Dl controls emissions
from a coarse ore dryer and transfer points.  Emissions from these
points are ducted through two separate dry cyclones before treatment by
a single wet scrubber.  A weighted average of the emissions from the two
                                 4-49

-------
dry cyclones  was taken to represent the total inlet flow to the wet
scrubber because no direct measure of the combined inlet was possible.
Total calculated inlet concentration averaged 22.2 g/DNm  (9.7 gr/dscf)
(Figure 4-18) while the outlet averaged 0.088 g/DNm3 (0.039 gr/dscf)
(Figure 4-18).  As shown in Figure 4-27, 30 percent of the inlet particles
were less than 6 microns and 4 percent less than 2 microns.   No data
were taken on scrubber outlet particle size.  The larger particle sizes
in the uncontrolled emissions from this dryer, in comparison with the
dryers at Plants B and C, reflects the size distribution of the coarse
ore fed to it.  The dryer at Plant D dried the ore before a final
grinding process, whereas the dryers at B and C were the final process
of the concentration step.
     Plant E processes iron ore mined from an open pit operation.
Processing at Plant E involves the crushing, concentrating, and pel-
letizing of the iron ore (hematite and magnetite combination).  The
plant uses wet scrubbers (2.5-kPa (10-inch) pressure drop) to control
emissions from crushing and pelletizing operations.   A wet scrubber
controlling emissions from the secondary crusher, secondary ore bin,
vibrating screen and screen undersize, and a conveyor for ore to the
tertiary ore bin was tested by EPA.   As shown in Figure 4-19, the
emissions from this scrubber averaged 0.026 g/DNm  (0.011 gr/dscf).
Uncontrolled emissions and particle size distributions in the combined
or individual inlet ducts were not measured.
     Plant F also processes iron ore mined from an open pit operation.
This plant was tested on two occasions, once in 1973 and again in 1978
after the wet scrubbers had been replaced by baghouses.  The 1973 test
measured emissions from a wet scrubber (pressure drop unknown)
controlling secondary and tertiary crushing operations.  Emissions from
the wet scrubber, tested in 1973, were 0.011 g/DNm  (0.005 gr/dscf).
Only one replicate was run, and no measurement of inlet particle size or
concentration were taken.
     Plant H processed bauxite imported from Jamaica during the test
period.   Wet scrubber HI controlled emissions from a transfer point at a
ship unloading facility.   Only one inlet and outlet concentration
                                 4-50

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measurement was taken.  Values were 2.61 and 0.039 g/DNm  (1.14 and
0.017  gr/dscf), as  shown  in  Figures 4-24 and 4-25, respectively.
     As  noted  in  the  text above  and shown in Figure 4-19, the emissions
from dryers at Plants C and  D were considerably higher than from all
other  scrubbers tested.   Because the  scrubbers'tested at these dryers
were relatively low pressure drop scrubbers, the performance of higher
energy wet scrubbers  was  modeled upon the characteristics of dryer
exhausts at Plants  B, C,  and D.  The  rationale for this modelling is
consistent with the method of applying worst case conditions as discussed
in the introduction to this  section;  the results are presented in
Section 4.6.
4.5.2  Visible Emissions  Data:   Wet Scrubbers
     In addition  to particulate  concentration measurements taken in
accordance with EPA Method 5 procedures, visible emission observations
were also made during the emissions tests described above.  Table 4-3
presents a summary  of EPA Method 9 data.  There is no direct relationship
between the opacity data  shown for the various wet scrubbers and the
outlet emission concentrations.  For  example, scrubber B3 averaged
                                   3
outlet concentrations of  0.02 g/DNm   (0.009 gr/dscf) and opacity readings
as high as 24  percent while  scrubber  C4 averaged outlet concentrations
             o
of 0.16 g/DNm  (0.067 gr/dscf) with opacity readings ranging from 0 to
5 percent.
     Section 4.8 will present visible emission data for fugitive emissions
at hoods and other  pickup points at metallic and non-metallic minerals
plants.
4.6  MATHEMATICAL MODELLING  OF VENTURI SCRUBBER EFFICIENCY
     Although  fabric  filter  baghouses will most often show superior
performance in removing small size particles, there are worst-case
scenarios possible  as discussed  in Sections 4.4 and 4.5 where a high
pressure drop wet scrubber may be the preferred type of control equipment.
When high moisture  ore is processed,  the resulting emissions mciy blind
the fabric filter in the  baghouse resulting in increased pressure drop
and decreased  performance due to incomplete cleaning of the bags.   Both
Plant  C and Plant I process  high moisture ore though only Plant I uses a
                                 4-52

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-------
baghouse to control emissions.   During testing at Plant I, the fabric
filter bags required manual air-lancing between test runs in order to
keep the pressure drop within acceptable levels.  This rapid "blinding"
of the bags which prevented proper cleaning by the pulse jet system
presumably occurred as a result of the condensation of moisture from the
warm, wet ore.
     A second effect of high moisture conditions is the suppression of
emissions from ore processing operations.  As was pointed out in
Section 4.4.1, the high moisture conditions under which Plant C operates
suppressed uncontrolled emissions to levels comparable to controlled
emissions at other metallic mineral plants.  Measurements at Plant I
also indicated low inlet concentrations.
     Because high pressure drop venturi scrubbers were not available for
testing in the metallic mineral processing industry, it was decided to
compare the performance of 1.5-kPa (6-inch), 3.7-kPa (15-inch), and
7.5-kPa (30-inch) venturi scrubbers utilizing a modelling program developed
by Sparks (1978).  The predictions of this model have been compared to
                                   !                            >
the performance of actual scrubbers controlling fly ash particles of
various types.  This model predicts particle penetration to within
±10 percent of actual values (95 percent confidence interval) (Sparks,
1981).  Performance of the venturi scrubber was modelled under two sets
of circumstances.  The first set of conditions involved the use of the
particle size data and uncontrolled particulate emission concentration
as measured from a secondary crusher at Plant I.  The particle size data
at Plant I are typical of values found in the metallic mineral industry.
     The second set of conditions involved the use of particle size data
and uncontrolled emission concentrations taken at Plant Q.  The particle
sizes measured at Baghouse Q2  were the smallest measured at any site
with a comparable level of emissions in either the metallic or
non-metallic industry.  There is good reason to expect this to have been
the case.  The fluid energy mill tested at Plant Q is a dry size-
reduction operation that reduces material to an approximate diameter of
1 to 20 microns, a smaller diameter than is typically required in the
metallic mineral processing industry.  Because the fluid energy mill
                                 4-55

-------
pneumatically classifies material, the exhaust stream from this operation
would be expected to contain a significantly higher percentage of submicron
material than an exhaust stream from a typical crushing operation.   The
combination of uncontrolled emission concentrations and small particle
size at Baghouse Q2 provide the most difficult control case tested in
the non-metal!ics industry and reflect conditions worse than any
likely to occur in the future in the metallic minerals industry.
     The parameters used in modelling the performance of venturi scrubbers
are presented in Appendix C.  Where more than one particle size test was
run at a facility, the distribution showing the lowest median particle
size was used.  Appendix C also presents a verification of this model
against known conditions and performance data for the metallic mineral
industry.               ,
     Table 4-4 summarizes the results of this modelling.   As expected
the control efficiency (defined in the program used as 100 (1-p) where p
is the proportional particle penetration integrated over the particle
size distribution) is directly related to pressure drop.   At any given
pressure drop the control efficiency is greater for Plant I than for
Plant Q.   Under worst-case conditions represented by Plant Q, a 1.5-kPa
                                                                     3
(6 inch) venturi scrubber could achieve emission levels of 0.34 g/DNm
(0.15 gr/dscf); a 3.7-kPa (15 inch) venturi scrubber could achieve
0.14 g/DNm3 (0.06 gr/dscf).  Under more typical industry conditions
represented By Plant I, the venturi scrubber would provide more effective
control both in terms of the percent reduced and the absolute levels
achieved.  The baghouse at Q2 provided considerably better performance
under dry conditions than that predicted for a 7.5-kPa (30-inch) venturi
scrubber.
     Because the dryers used in the metallic mineral industry might have
similar problems with high moisture and because no data were available
on the use of high pressure drop scrubbers on dryers, a separate set of
modelling exercises as undertaken for dryers at Plant B, C, and D.   The
modelling parameters are detailed in Appendix C and the results are
summarized in Table 4-5.  As shown in this table, all the dryers would
average emissions of 0.05 g/DNm3 (0.02 gr/dscf) or less with a 7.5-kPa
(30-inch) venturi scrubber.
                                 4-56

-------



















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4; 7  EXHAUST SYSTEMS AND DUCTING
     The efficient and effective control of participate emissions requires
the capture of these emissions at the source of generation.   Capture
requires the proper design of a hood and ducting system.  Such a system
usually consists of a close-fitting hood surrounding the point at which
particle-laden air is discharged into a ducting system and carried to a
collection device by one or more exhaust fans.
     Design of an exhaust system requires careful planning in order to
ensure that air flow is sufficient to pick up all emissions and convey
them to the collector.  On the other hand, excessive air flow rate will
overburden the system and increase capital and operating costs.  Recom-
mended exhaust requirements for several of the operations involved in
metallic minerals processing are presented in Table 4-6.
     The hood should be designed so that the process machinery can be
easily reached.  This can usually be achieved by installing doors in
sheet metal hoods.  Other enclosures that consist of of heavy rubber
matting or other pliable material provide fewer problems for access.
These materials, however, are not suitable where the hood or enclosure
is to be an integral, free standing structure.
     Dust must move through ductwork with sufficient velocity to avoid
settling.  Recommended minimum duct velocities have been published and
are given in Table 4-7.  The system must be as compact as possible to
minimize friction and branching losses and to reduce operating (power)
costs.  For this reason, the collection devices should be placed as
close as possible to the sources of emissions.  Care must be taken to
ensure that the ducts are designed with a balanced duct or static pressure.
This means choosing duct sizes that result in a static pressure balance
at each junction, achieving the desired air volume in each branch duct.
     The following sections describe several of the process emission
sources and how they can be enclosed and exhausted.  Various guidelines
for the design of the exhaust and ducting systems are also mentioned.
4.7.1  Conveyor Belt Dust Control
     Dust generation occurs primarily at the point where ore is trans-
ferred from one conveyor to another especially where a drop is involved
                                 4-59

-------
            Table 4-6.   EXHAUST REQUIREMENTS FOR METALLIC MINERAL
                           PROCESSING OPERATIONS3
 Operation
Exhaust arrangement
                  Remarks
Conveyor belts
Hoods at transfer.
points enclosed as
much as possible
Bucket elevator  Tight casing
Grinders,
crushers
Enclosure
For belt speeds less than 1 m/sec
(200 ft/min), gas flow (Q) should be
0.5 m3/sec for each meter of belt
width (350 ftVmin for each ft of
belt width) with at least 0.75 m/sec
(150 ft/min) gas velocity through
openings.   For belt speeds greater
than 1 m/sec (200 ft/min), Q = 0.7
mVsec for each meter of belt width
(500 ftVmin per each foot of belt
width) with at least 1 m/sec (200
ft/min) gas velocity through
remaining openings.  Also note the
additional exhaust requirements
on Figure 4-28 for material drops
greater than 1 meter (3 feet).

For 0.05 ms/sec for each square
meter (100 ftVmin per square foot)
of elevator casing cross section
(exhaust near elevator top and also
vent at bottom if over 10.7 m (35
ft) high).

Gas velocity of 1 m/sec (200 ft/min)
to 2.5 m/sec through openings.
JDanielson (1973, p. 31).
                                    4-60

-------
               Table 4-7.  RECOMMENDED MINIMUM DUCT VELOCITIES'
Nature of contaminant
              Examples
Dust velocity
m/sec(ft/min)
Gases, vapors, smokes
fumes, and very light
dusts

Medium-density dry
dust

Average industrial
dust

Heavy dusts
All gases, vapors, and smokes;
zinc and aluminum oxide fumes;
wood, flour, and cotton lint

Buffing lint; sawdust; grain,
rubber, and plastic dust

Sandblast and grinding dust,
wood shavings, cement dust

Lead, and foundry shakeout
dusts; metal turnings
 10
(2000)
 15      (3000)


 20      (4000)


 25      (5000)
aDanielson (1973, p. 50).
                                    4-61

-------
which allows falling dust to become airborne.   Ideally,  the area including
the head pulley of the feeding conveyor and the tail  pulley of the
receiving conveyor are enclosed.   Two schematics of proposed enclosures
with hooding points are represented in Figure 4-28 (American
Conference of Governmental Industrial Hygenists (ACGIH), 1976, p.  5-33).
One system is designed for less than a 1 m (3 ft) drop between the
belts, the other designed for greater than aim drop.  The first of the
two is seen most frequently in the industry.   Ore is discharged into a
small bin which feeds the pickup belt below.   A hood located over the
bin recovers any discharge created in the process of transferring the
ore.  The receiving belt is placed just below the outlet of the bin so
that it, in effect, "drags" the ore into it.   In addition, a rubber
skirt is usually fitted at the belt opening where discharge from the bin
occurs.  The skirt narrows the opening through which particles can
escape, in effect causing the crushed ore in the hopper discharge to act
as a curtain that traps dust.  Ideally, the open area at the.bin discharge
should be reduced to 0.16 m2/m (0.2 ft2/ft) of belt width.
     These transfer points should be designed so that a minimum indraft
of 0.75 to 1 m/sec (150 to 200 fpm) is provided at all openings when
conveyor belt speeds of under 1 m/sec (200 fpm) are encountered.  Because
conveyor belts carrying ore act much like a fan, as conveyor belt speeds
increase it is good practice to design air velocities into openings of
conveyor enclosures at least equal to belt speeds (Laird, 1980).  Minimum
volumetric flow should be 0.5 m3/sec/m (350 cfm/ft) of belt width for
belt speeds under 1 m/sec (200 ft/min) or 0.7 m3/sec/m (500 cfm/ft) of
belt width for belt speeds over 1 m/sec (200 ft/min).  Duct minimum
velocity should be 18 m/sec (3,500 ft/min) (ACGIH, 1976, p. 5-33).
4.7.2  Crushers and Dry Grinders
     Crushing equipment generates a significant amount of dust emissions
in the mineral processing industry.  The wide range of sizes and types
of crushing equipment and the variability of dust emissions require
design specifications for exhaust systems that vary from plant to
plant.  Though dry grinding also constitutes a significant emission source
at a few plants, dry grinding operations are not expected at future
                                 4-62

-------
                                          To Central
                                           ftevlce
                           24" »1n|
                                              Rubber
                                               Skirt
                                (2)
Greater than 31 fall  use additional
control exhaust as shown (A)
at following rates:

   Belt Width    Exhaust

    12"-36"  .  0=700 cfm
   above 36"    Q« lOOOcfm
                                      Conveyor Transfer
                                          2 x Belt Width
                                     1/3 Belt Width-
                                        Rubber Skirt
2" Clearance For
  Load On Belt
                                                             24" m1n
                                  Chute to Belt Transfer
      Figure 4-28.  Methods of hooding conveyor transfer points (ACGIH.1976),

-------
metallic mineral processing operations.   Indraft velocities associated
with the hooding around these crushers and dry grinders should be
1 m/sec (200 ft/ min) (Danielson,,1973).
     For underground mining operations,  primary crushing often takes
place below ground.  The ore is crushed sufficiently to allow loading
into skips for elevation to the surface.  In some mines, the rock breaks
naturally into fragments small enough to allow direct loading into the
skips with primary crushing occurring at the surface.
     Surface primary crushers often have no hoods at the inlet but
usually are hooded at the outlet.  The crusher is often located in a pit
at the surface that is ventilated to the control equipment (see
Figure 4-29).  The pits are maintained at negative pressure.  A truck
dump over or near the primary crusher, as depicted in Figure 4-29, is
often enclosed in a building.  The truck dump area of the building can
then be exhausted to a collection device.
     In controlling crushers, the objective is to enclose the source as
well as possible.  In secondary and tertiary crushers, this is performed
by completely enclosing the inlet to the crushers with hoods fitted with
maintenance doors.  The outlet of the crusher has an apron feeder which
is enclosed and ducted to a collection device.  Figure 4-30 is a typical
exhaust system for a secondary or tertiary crusher.
     Ductwork follows the general design guidelines for other process
equipment ducting.  For impact crushers or grinders, exhaust volumes may
range from 1.9 to 3.8-m3/sec (4,000 to 8,000 cfm).  For compression type
                                  o
crushers, an exhaust rate of 0.7 m/sec per meter (500 cfm/ft) of
discharge opening is sufficient (ACGIH, 1976, p. 10-1 to 11-28).  The
width of the discharge opening will approximate the width of the
receiving conveyor.  For either type of crusher, pickup should be applied
downstream of the crusher for a distance of at least 3.5 times the width
of the receiving conveyor (Environmental Protection Agency, 1979).
4.7.3  Screens
     In controlling dust emissions from screens, the best technique is
to fully enclose the screens and undersize hopper with a hood.  The
screen discharge is then ducted,to one or more control devices.  Often,
screening takes place immediately prior to a crushing operation and the
screens are enclosed by the crusher's dust hood.

                                 4-64

-------
To Collection
    Device
               Surge Bin
                       (oj
Conveyor Belt
                                To Collection
                                    Device
       Figure 4-29.  Typical exhaust system for a primary crusherj.


                                            4-65

-------
                                                  To Collection
                                                     Device
                                  Maintenance Door


                                      Hood
Feed Conveyor/-*-
           /-"I'D
      Surge Bin
         Apron
         Feeder
Figure 4-30.  Typical exhaust system for a secondary
              or tertiary crusher.
                              4-66

-------
     Flat deck and cylindrical screens (the two most common types),  with
their associated exhaust systems, are depicted in Figure 4-31.   Exhaust
flow rates vary with the surface area of the screen and a common value
is 0.2 (m3/sec)/m2 (50 cfm/ft2) of screen area (ACGIH, 1976, p.  5-34).
No change in this figure is associated with multiple decks.  In exhaust
systems for flat deck screens, a flow rate of 1.0 m3/sec/m  (200 cfm/ft )
of hood opening and a duct velocity minimum of 17.8 m/sec (3,500 ft/min)
                                                      3      2
is common.  In cylindrical screens flow rates of 0.5 m /sec/m
(100 cfm/ft2) of circular cross section of screen and duct velocity of
17.8 m/sec (3,500 ft/min) are common (ACGIH, 1976, p. 5-34).
4.7.4  Raw Materials and Product Storage in Bins
     Materials at intermediate stages of processing often are stored in
bins or silos.  An enclosure with a hood is located as far from the
entrance to the bin as possible.  Figure 4-32 is a representation of
common methods of exhausting dust from entrances of storage facilities.
     As with most other process equipment exhaust systems, minimum
indraft velocity is 1.0 m3/sec/m2 (200 cfm/ft ) for all open areas.   A
duct velocity of 17.8 m/sec (3,500 ft/min) minimum is also the rule
(ACGIH, 1976, p. 5-31).  Induced drafts as a function of conveyor belt
speeds must also be considered as noted in Section 4.7.4.  Handling of
dry and dusty material may also increase air flow requirements.
     Volumetric flow rates with respect to belt speed are:
     «    0.5 m3/sec/m (350 cfm/ft) of belt width for belt speeds of
          less than 1 m/sec (200 ft/min)
     g    0.7 m3/sec/m (500 cfm/ft) of belt width for belt speeds of
          more than 1 m/sec (200 ft/min).
4.7.5  Product Handling
     Dust suppression and collection devices are used to control dust
generated by product handling operations.  Often, concentrate is loaded
as filter cake which contains sufficient moisture to suppress dust
during this operation.  Where dry, dusty products are handled, baghouses
are commonly used and not only provide particulate control but also
recover valuable product.
                                 4-67

-------
                      T° ^Device1™
            Feed
                    Flexible Connection

                    Top Ttke-off Preferred

                                     ^Oversize

                                  s£\
Complete Enclosure-*
  Flow Rate.(Q)
                          FLAT DECK SCREEN
200 cfin/ft  through hood openings,  but not less
than 50 cfm/ft* screen area;  No Increase for
multiple decks.  Duct velocity « 3,500 fpm
minimum.
                                 To Collection
                                      Device
                            45° m1n
                                     Feed
Complete .^
Enclosure
^-k^5"^
j Screen
ff
f
                 Oversize
                             CYLINDRICAL SCREEN


                 TOO cfm/ft2 circular cross section of screen; at least
                 400 cfm/ft2 of enclosure opening.  Duct velocity -
                 3,500 fpm minimum.
                  Figure 4-31.  Screening exhaust systems,
                                     4-68

-------
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                                    4-69

-------
     Particulate emissions from truck and railcar loading of coarse
material can be minimized by reducing the open space from the silo or
bin to the shipping vehicle that the material must fall through.
Shrouds, telescoping feed tubes, and windbreaks can further reduce the
fugitive emissions from this intermittent source.  Particulate emissions
from loading of fine material into either trucks or railroad car can be
controlled by an exhaust system vented to an emissions control system.
The system is similar to the system described above for controlling bin
or hopper transfer points (see Figure 4-32).  The material is fed through
one of the vehicle's openings and the exhaust connection is normally at
another opening.  The system should be designed with a minimum amount of
open area around the periphery of the feed chute and the exhaust duct.
The system can also be exhausted through a double concentric tube with
material fed through the inner tube and air exhausted through the outer
tube.
     Where product is being loaded into open rail cars or trucks other
emission control arrangements are necessary.  Figure 4-33 is a repre-
sentation of such a-system currently in use in Arizona.  Trucks unload
concentrate into a hopper that is enclosed and exhausted to a control
device.  The concentrate is then fed via a conveyor belt to a
telescoping chute.  The conveyor belt and chute are also ducted to the
same collection device as the truck.hopper.
4.7.6  DryTng of Product
     Product is dried to reduce the moisture content of the filter cake
or concentrate.  Concentrate dryers usually involve direct contact
between the drying material and the heating source.  Dust generated in
the drying process passes directly into a duct located at the exit of
the dryer and is then removed from the airstream by a control device.
                                                            2
The flow rates through the duct work range from 1.8 to 7.1 m /sec
(4,000 to 15,000 cfm) at plants that were visited.  In some systems
product released into the exhaust stream from the dryer is returned to
the process after collection by dry cyclones and/or wet scrubbers.
                                 4-70

-------
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4-71

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4.8  Performance Data for Exhaust Systems
     Concurrently with most of the tests of wet scrubber and baghouse
performance, the effectiveness of exhaust systems, hoods, and other
capture devices was tested.  After analysis of air flow rates taken
during the Method 5 tests, it became apparent that some hood systems
were not meeting the minimum design criteria outlined above for air
velocities at hood openings or emission null points.   In most cases
these problems could be avoided in new facilities by proper positioning
of the hood or the more complete enclosure of a source rather than
increasing the actual flow rate.  Data are not reported for points with
design deficiences.
     Effectiveness of exhaust systems is measured in terms of opacity of
visible emissions escaping capture at the crucial junction between the
process equipment and the inlet to the ducting system (the pickup point)
by EPA Method 9.  Method 9, described in Section 4.3.2, measures opacity
at 15-second intervals on a scale from 0 to 100.  Readings are then
averaged over 6-minute periods.              *
     Table 4-8 presents results of the tests by Method 9 for emission
sources controlled by wet scrubbers and baghouses in both the metallic
and non-metallic mineral industry.  Three additional  plants (R, S, T)
are listed in Table 4-8.  These plants were observed as part of EPA's
test program for non-metallic minerals.   Plant R processed gypsum; Plant
S, mica; and Plant T, talc.  Test sites from the non-metallic mineral
processing industry are included here because the techniques for capturing
emissions from operations in the metallic and non-metallic industry are
similar.
     In most instances, essentially no visible emissions were observed
at adequately hooded or enclosed process facilities.   The data indicate
that properly designed facilities can meet visible emission limits of
10 percent opacity calculated as a 6-minute average.
4-9.   ELECTROSTATIC PRECIPITATORS
     As noted in the introduction to this chapter, the use of electrostatic
precipitators (ESP's) in the metallic mineral industries has been confined
to high temperature, high flow exhaust streams from calcining and
pelletizing operations.  The use of ESP's is probably not necessary for
                                 4-72

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the types of operations discussed in this document and their performance
can be duplicated with less expensive devices.  However, because ESP's
are highly effective particulate emission control devices, their use is
possible with the emissions from metallic mineral processes and a brief
description is thus provided.
     ESP's operate by electrically charging incoming particles by bombarding
them with gaseous ions or electrons formed by high voltage corona discharge.
An electrostatic field attracts the ions to oppositely charged plates or
collection electrodes.  This process can take place in one, two, or
multiple-stage operations.  A two-stage ESP is depicted in Figure 4-34.
     ESP's operate with very low pressure drops, and high volumetric flow
rates and temperatures.  ESP's also have no moving parts and,
theoretically, have no lower limit on the size of particles that can be
collected.  Collection efficiencies of 99+ percent for 0.1 to 3 micron
particles can be readily achieved.
     Operating conditions for electrostatic precipitators are as follows
(Hesketh, 1974):
     •    Gas flow - 1 cfm to 2 x 106 cfm (.03-57,000 mVmin)
     t    Gas temperature - up to 1200°F (650°C)
     •    Gas pressure - up to 150 psi (1000 kPa)
     •    Gas velocity - 3 to 15 ft/sec (up to 50 ft/sec in special
            units) (1 to 5 m/sec (up to 15 m/sec))
     •    Pressure drop - 0.1 to 0.5 in. of water per section
            (0.02-0.1 kPa)
     •    Particles removed - 0.1 to 200 microns
     •    Particle inlet concentration - 0.15 x 10"3 to 15 lb/1,000 ft3
            (2.3 x 10~3 to 2.3 x 102 gram/DNm3)
     •    Treatment sequence - 1 to 10 sections in series
     •    Power supply - 50,000 to 70,000 Vdc (up to 100,000 V in some
            units)
     •    Discharge electrodes - up to 0.109 in. (0.025 mm) diameter
            coppered steel wires
     There are several drawbacks to electrostatic precipitation, including
high initial cost and necessity for frequent maintenance.   The initial
cost is the highest in the air pollution control equipment market.
                                 4-76

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4-77

-------
4.10  CONCLUSIONS FROM TEST AND MODELLING DATA
     Several conclusions are justified after a review of the test data
in this chapter.  A comparison of particle sizes ranges for the metallic
and non-metallic facilities indicates similar distributions.  Table 4-9
includes data on the percentage of particles under 5 microns at all
processes  tested.  This figure ranged from 2 to 92 percent with an
average of 36 percent for metallic mineral processes.  Excluding the
particle size data from facilities Cl, C2, and C3, which are of minimal
significance because of the very low uncontrolled emission rates, the
range for  the metallic facilities was from 2 to 87 percent with an
average of 28 percent.  In either case the particle size range for
non-metallic facilities indicated smaller particles at these facilities.
The percentage of particles below 5 microns ranged from 10 to 92 percent
and averaged 48 percent.
     Engineering specifications for control equipment for use in the
metallic mineral industry typically assume uncontrolled emission rates
of 11.4 to 22.9 g/DNm3 (5 to 10 gr/dscf).  This range of values is
significantly in excess of most of the concentrations measured in this
study.  Table 4-9 summarizes all the uncontrolled emission rates from
both single and combined unit processes or processing steps measured in
the studies described.  Of the points measured only four exceeded
           •3
11.4 g/DNm  (5 gr/dscf).  These points included the dryer at Plant D,
the primary crusher at Plant K, the pebble mill at Plant 0 and a roller
mill at Plant Q.  Over one half of the points tested showed
                              3
concentrations below 2.3 g/DNm  (1.0 gr/dscf).
     The overall average of the uncontrolled emission concentration
measured at ducts venting individual process steps in the metallic
                                                         o
minerals industry (as marked in Table 4-8) was 1.99 g/DNm  (0.87 gr/dscf).
When breaking out emission data by emission source type, certain patterns
were noted.  Dryers showed the highest uncontrolled emission levels with
                                      o
an average concentration of 9.38 g/DNm  (4.10 gr/dscf).   Crushers showed
                                                            3
an average uncontrolled emission concentration of 2.04 g/DNm
(0.89 gr/dscf).   Transfer points and product loadout operations showed
similar emission levels of 0.66 and 0.55 g/DNm3 (0.29 and 0.24 gr/dscf),
                                 4-78

-------













 
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respectively.   Finally, screens and fine ore bins showed very Tow emission
rates of 0.11 and 0.007 g/DNm3 (0.05 and 0.003 gr/dscf), respectively.
     These low uncontrolled emission levels might be interpreted as
evidence that some sites are unnecessarily diluting process emissions.
However, it must be recognized that air flow requirements are most often
determined by the necessity to maintain minimum air velocities and flow
rates at the hoods or pickup points as required by MSHA regulations.
Careful attention should be paid to the design of hoods in order to
maximize the efficient enclosure of the point of emissions and to
minimize the air flow requirements and consequent energy use.
     In contrast to the metallic minerals facilities, non-metallic
                                                         Q
facilities averaged an uncontrolled emission of 8.2 g/DNm  (3.6 gr/dscf).
This higher emission level coupled with the generally smaller particle
sizes as exemplified in Plant  P and Q again support the introductory
comment that the non-metallic  facilities provided more difficult control
conditions than those encountered in the metallic minerals industry.
     In general a review of the data presented in this chapter  indicates
that a wide variety of conditions were sampled in these tests.
Uncontrolled emission  rates ranged from almost immeasurably  low, as in
the case of some operations at Plant C, to  close to the maximum design
levels, as in the case of  the  dryer at Plant D.  Mean particle  size
ranged  from less than  2 microns to greater  than 20 microns.  Because of
the  range of possible  conditions, control equipment should be applied to
a specific facility with an understanding of the emission characteristics
of the  operation that  may  require actual testing of this facility.
     The  approach  in this  chapter and  throughout this document  is  to
present the worst  case conditions and  to judge the  effectiveness  of
various approaches  in  that light.   The necessity of  finding  performance
levels  that  are achievable in the widest possible  range of circumstances
 in the  industry compel us  to  view  the  entire  industry  in terms  of worst
case conditions.   This approach, however,  should not obscure the  fact
 that much of the industry may operate  under less  adverse circumstances
 and  thus  may properly  apply a variety  of  techniques  to  achieve  prescribed
 goals.   The  purpose of this chapter is to  outline  achievable levels of
 performance,  but not to dictate the methods for achieving  these levels.
                                  4-83

-------
     A  review  of the tests of baghouses at metallic and non-metallic
facilities demonstrates that baghouses can easily attain emission levels
             3
of 0.05 g/DNm   (0.02 gr/dscf) under a wide variety of circumstances.
Manufacturers  of baghouses routinely guarantee performance of properly
                                                           o
designed baghouses to meet emission standards of 0.05 g/DNm  (0.02 gr/dscf)
(Adams, 1980;  and Skalos, 1980).
     The tests of wet scrubbers at metallic minerals facilities indicate
that, at many  operations tested, wet scrubbers with pressure drops as
                                                                     3
low as  1.5 kPa (6 inches) could meet emission levels below 0.05 g/DNm
(0.02 gr/dscf).  Exceptions are the dryers at Plants C and D.  Because
these facilities use relatively low-energy wet scrubbers, modelling
exercises were undertaken to predict the performance of higher pressure
drop venturi scrubbers given the uncontrolled emission characteristics
at these facilities.  These modelling exercises show that these facilities
could meet 0.05 g/DNm3 (0.02 gr/dscf) with a 7.5-kPa (30-inch) venturi
scrubber.
     Given the potential problems with moisture condensation in dryer
exhaust, wet scrubbers may be preferred to baghouses for the control of
emissions under these circumstances.  In addition, in situations where
warm moist ore extracted from underground mines is processed at surface
temperatures significantly below mine temperatures, moisture condensation
may preclude the use of baghouses.   Modelling of the performance of
venturi scrubbers given the emission characteristics at Plant I (which
processed high moisture ore from underground mines) was reported in this
chapter.  These results showed that both 1.5- and 3.7-kPa (6- and 15-inch)
wet scrubbers  could meet a 0.05 g/DNm  (0.02 gr/dscf) emission level.
     Modelling of the performance of venturi scrubbers given worst case
conditions was performed and reported in this chapter.   Worst case
conditions as  observed at Plant Q were determined on the basis of particle
size distribution and uncontrolled emission rate.   The emission particle
sizes from the fluid energy mill at Plant Q would be smaller than typically
encountered in the metallic mineral industry because this operation
processes  material  to a smaller size than do dry operations in the
metallic mineral industry.   Given these worst case conditions, a 1.5-kPa
                                                                o
(6-inch) wet scrubber will  allow an emission level of 0.34 g/DNm

-------
CO.15 gr/dscf).   A 3.7-kPa (15-inch) venturi scrubber would allow
emission levels  of 0.14 g/DNm3 (0.06 gr/dscf).   As indicated by the test
results at this  facility, a baghouse can attain the emission levels
below 0.05 g/DNm3 (0.02 gr/dscf).
     This raises the following hypothetical question:  What if the
particle size distribution found at the fluid energy mill  occurred under
high moisture conditions which precluded use of a baghouse?  Given the
conditions present at Plant Q, modelling of the performance of 7.5-kPa
(30-inch) venturi scrubbers indicated that it would give an emission
level of 0.05 g/DNm3 (0.02 gr/dscf).  Because high moisture conditions
would suppress uncontrolled emission levels as shown in Plants I and C,
uncontrolled emission rates as high as those at Plant Q would not be
expected and, in turn, wet scrubber emissions would be lower.
     In conclusion, though the metallic mineral processing industry
encompasses a wide variety of processes and ore types, the fundamental
parameters of uncontrolled emission rate and particle size distribution
(as demonstrated by the tests in this chapter) indicate conditions
amenable to commonly available methods of particulate emission control.

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4.9  REFERENCES FOR CHAPTER 4
Adams, J., American Air Filter Company.  1980.  Telephone conversation
     with E. Monnig, TRW.  September 26.  Emission limit guarantees for
     baghouse performance.

American Conference of Governmental Industrial Hygienists (ACGIH).
     1976.  Industrial Ventilation - A Manual of Recommended Practice.
     Lansing, Michigan,  pp. 4-1-4-21; 5-29-5-34.

Danielson, J. A., 1973.  Air Pollution Engineering Manual (AP-40),
     Environmental Protection Agency, Research Triangle Park,
     North Carolina,  p. 31.

Ducon Inc.  1978.  Dynamic Gas Scrubber, Type UW-4, Model IV.  No.
     W-7578.  Mineola, New York.  8p.

Environmental Protection Agency (EPA), 1979 (March).  Non-Metallic
     Mineral Processing Plants - Background Information for Proposed
     Emission Standards.  Draft Document.  Research Triangle Park,
     North Carolina,  p. 4-1 to 4-5.

Hesketh, H.E..  1974.  Understanding and Controlling Air Pollution.  Ann
     Arbor Science Publications.  Ann Arbor, Michigan.

Laird, F. J., Anaconda Copper Company, 1980.  Letter to S. T. Cuffe,
     Environmental Protection Agency.  December 23.  Comments on emission
     control techniques in the metallic mineral industries.

Skalos, C., Dravo Corporation.  1980.  Telephone conversation with
     E. Monnig, TRW.  September 26.  Emission limit guarantees for
     baghouse performance.

Sparks, L. E., 1978.  SR-52 Programmable Calculator Programs for Venturi
     Scrubbers and Electrostatic Precipitators.  EPA/600/7-78-026.
     Environmental Protection Agency.  Research Triangle Park,
     North Carolina, pp. 3-28.

Sparks, L.E., Environmental Protection Agency.  1981.  Telephone
     conversation with E. Monnig, TRW.  February 18.  Precision of
     scrubber model.

Theodore, L. and A. J. Buonicore, 1978.  Control of Particulate Emissions.
     Environmental Protection Agency, Research Triangle Park,
     North Carolina, p. 5-19.

Usis, A., W. W. Sly Manufacturing Co.  1978.  Telephone conversation
     with R. Greenberg, GCA.  June 16.  Air-to-cloth ratio for baghouses.
                                 4-86

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                    5.   MODIFICATIONS AND RECONSTRUCTIONS

5.1  MODIFICATION
     A metallic mineral processing plant is composed of combinations of
crushers, grinding mills, screens, dryers, conveyor transfer points, ore
storage areas, and product handling operations.   For a change to be
termed a modification,  it must result in an increase in emissions from
any one of these process operations.
     As defined in 40 CFR 60.14, the following physical or operational
changes are not considered modifications to existing metallic mineral
processing plants irrespective of any change in the emission rate:
     A.  Changes determined to be routine maintenance, repair or
replacement.
     B.  An increase in the production rate if that increase can be
accomplished without a capital expenditure exceeding the existing
facility's IRS Annual Asset Guideline repair allowance of 6.5 percent
per year.
     C.  An increase in the hours of operation.
     D.  Use of an alternative raw material if the existing facility was
designed to accomodate such material.  Because process equipment
(crushers, screens, conveyors, etc.) are designed to accomodate a variety
of rock types, any change in raw material feed would probably not be
considered a modification.
     E.  The addition or use of any air pollution control system except
when a system is removed or replaced with a system considered to be less
effective.
     F.  The relocation or change in ownership of an existing facility.
     The expected impact of the modification provision on existing
metallic mineral processing facilities should be very slight.  No

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condition is currently foreseen that would allow an existing metallic
mineral processing facility to be modified under this definition.
Whether a change is a modification or not shall be determined by the
Division of Stationary Source Enforcement (DSSE) and the appropriate EPA
Regional Office.
     When expansions at existing plants take place, usually a completely
new crushing/grinding line is added (with the possible exception of the
primary crusher).  Such an increase in production would not be considered
a modification but rather a series of new sources.  Primary crushing
operations at metallic mineral plants usually operate below 100 percent
capacity and are capable of handling increased throughput without
additional equipment.  Under (B) above, an increase in production at the
primary crusher would not be considered a modification.
5.2  RECONSTRUCTION
     The reconstruction provision is applicable only where replacement
of components of an existing facility exceeds 50 percent of the fixed
capital cost that would be required to construct a similar new facility
and air pollution control systems are shown to be technologically and
economically feasible.  For the metallic mineral industries, replacement
or refurbishing of equipment parts subject to high abrasion and impact
such as crushing surfaces, screening surfaces, and conveyor belts are
performed on a regular basis and could be considered routine maintenance.
The cumulative cost of these repairs to any one piece of equipment over
a period of time could exceed 50 percent of the fixed capital cost of
entirely new equipment.   Whether such actions constitute reconstructions
shall be determined by DSSE and the appropriate Regional office.
                                 5-2

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                  6.   MODEL PLANTS AND REGULATORY OPTIONS

6.1  INTRODUCTION
     Chapter 4 presented various technologies available for the control
of particulate emissions.  These control technologies form the basis for
the regulatory alternatives available for the proposed new source perfor-
mance standards.   In order to evaluate the environmental and economic
impacts of the regulatory alternatives, an analysis of "model plants"
has been used.  Model plants have been selected for each of the ten
metallic ore processing industries that are expected to show growth in
processing capacity in the next 5 years.  These model plants are
representative of the expected population of new or expanded metallic
mineral processing plants that will be subject to the standards.
6.2  MODEL PLANTS                           • '       ,
     Although there are variations in the processes used for the different
minerals, there are operations that are common to various aspects of the
metallic mineral processing industries.  An all-inclusive model facility
can be depicted which includes all the particle-emitting processes
common to the industry.  All other model plants are subsets of this
all-inclusive facility.  It should be stressed that it is highly unlikely
that any new metallic mineral processing facility will look exactly  like
this all-inclusive facility or its subsets.  In general, these models
overestimate the actual  impacts.  As noted  in Chapter 3, increased use
of wet,grinding processes  is possible in the future which would reduce
the application of control technology at metallic mineral plants.
However, all  new metallic  mineral facilities will contain at  least some
of the  facilities described in this model.

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6.2.1  Inclusive Model Facility
     The inclusive model facility includes all of the usual processing
equipment and procedures that produce particulate emissions.   All the
sources of particle emissions can be classified and assigned an emission
point number.  In a single process line there are a total of 23 emission
points at the inclusive model facility.  Larger plants may run several
parallel lines and will contain more than 23 emission points.
Figure 6-1 presents a diagram of the model including all 23 labelled
emission points.  These numbers will remain constant throughout the
discussion of model plants for each emission point.
     The number and size of individual processing equipment units at
each emission point can be adjusted to represent the range of total
facility production capacities found in the industry.  Eight different
production capacity facilities have been selected to represent the range
of production capacities found in the industry.  The eight capacities
are 23 Mg/hr (25 TPH), 45 Mg/hr (50 TPH), 68 Mg/hr (75 TPH),  140 Mg/hr
(150 TPH), 270 Mg/hr (300 TPH), 540 Mg/hr (600 TPH), 1,100 Mg/hr
(1,200 TPH), and 2,200 Mg/hr (2,400 TPH).  The range of all ten individual
industries are covered by these eight capacities.  Table 6-1 presents
the eight capacities for the inclusive model facility and indicates the
size and number of process units at each emission point, as well as the
gas volumes.
6.2.2  Process Units
     As noted previously, there are a total of 23 emission points common
to the metallic mineral processing industries.  Although it is conceivable
that each of these emission sources could have one emission control
system, current industry practice indicates that several associated
emission points are ducted to a common control device.   For purposes of
analyzing the .environmental, economic and energy impacts, the process
equipment at the inclusive model facility have been grouped to form the
following process units.
     A.   Crushing unit - defined as a crusher and its associated
          dumping station, grizzly, screens, coarse ore storage bins,
          and conveyor belt transfer points.
                                 6-2

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     B.    Ore storage unit - defined as an enclosed ore storage area and
          associated conveyor belt transfer points if the area is
          isolated from the crushing unit.
     C.    Dryer unit - including the dryer and associated conveyor belt
          transfer points.
     D.    Product loadout unit - including all packaging, product bins,
          conveyor belt transfer points, and loadout mechanisms excluding
          ship loading facilities.
     Because the inclusive model facility contains emission points and
processes common to the whole industry, all ten individual industries
can be described and grouped as they relate to the inclusive facility.
The ten individual industries can be grouped into seven categories
according to the ways in which they vary from the model facility.  The
seven categories are keyed alphabetically and are as follows
     A.   no tertiary crushing, drying, or product loadout;
     B.   no secondary or tertiary crushing or drying;
     C.   no secondary or tertiary crushing, drying, or product loadout;
     D.   all-inclusive category;
     E.   no drying or product loadout;  .
     F.   no drying;
     G.   no primary, secondary or tertiary crushing or fine ore bins.
The ten industries showing growth rates correspond to the above
categories as follows
     A.   gold;
     B.   aluminum;
     C.   uranium;
     D.   copper, lead/zinc, molybdenum, tungsten;
     E.   silver;
     F.   iron;
     G.   titanium/zirconium.
Antimony, beryllium, titanium hard  rock,  and  vanadium ores are not
included because no growth in processing  capacity is projected for these
industries  (see Section 3.1);  Domestic production of nickel may  increase
in the future; however, this  increase will occur as a byproduct  of
copper production  in Minnesota.   Commercial development  of these  deposits
                                 6-8

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is not expected until after 1985 which is beyond the time frame covered
in this document.
6.3  REGULATORY ALTERNATIVES
     Chapter 4 presented the emission control technologies that can be
used to control particulate emissions from metallic mineral processing
plants.  Each of the control techniques form the basis for a regulatory
alternative for each process unit.  In order to evaluate the environmental
impacts, numerical emission limits can be selected that would represent
each of these regulatory alternatives.  These emission limits are derived
by applying the control equipment option and its efficiency to the
uncontrolled emission rate from each process unit.  Because any promul-
gated emission limits must be achievable by all anticipated sources
under all reasonable process conditions, the emission limit should
represent.the emission level achieved by the control technique option
under the most adverse control conditions.  Although the emission levels
represented by the alternatives are based on the performance of a specific
emission control device (for example, a 1.5-kPa (6-inches of water) wet
scrubber) under worst-case conditions, it must be emphasized that the
specified emission control device will achieve lower emission levels
under  less than worst case conditions.  The converse is also true.  The
specific emission limit represented by a regulatory alternative can
usually be attained  by control equipment designed for less rigorous
conditions than the  control equipment upon which the regulatory alterna-
tive  is based.
      Source test  data  indicate that the most adverse particulate control
conditions that could  be  expected in  the metallic mineral  industries  are
represented by an uncontrolled particulate emission concentration of
2.3 g/DNm3 (1.0 gr/dscf)  with a mean  particle  size  (x) of  1.5 \xn.  As
discussed in  Chapter 4, the 2.3 g/DNm3  (1.0  gr/dscf) concentration level
is not as  high as that currently  found  at some facilities; however, a
comparison of source test data with the  combined  factors  of  uncontrolled
emission  concentration and particle size  distribution indicates that  the
highest controlled  emission rates would occur  with  this  combination.
                                  6-9

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6.3.1  Regulatory Alternative 1
     One of the regulatory alternatives available for consideration is
the option of no new source performance standard(s).   This is the base-
line control level and is generally representative of the level of
control required by existing State Implementation Plan (SIP)
regulations.  Most states do not have specific regulations for the
metallic mineral processing industries.  Instead these facilities are
usually regulated under a miscellaneous industrial process regulation.
The typical state industrial process emission limits are derived from
the following equations:
                        30
30
             E=  4.1 x p0*67              E =  55 x p0-11 -40
Where p = production in tons/hr
      E = emissions in Ib/hr
     However, test data indicate that current controlled emission rates
at existing facilities are often actually less than allowed by SIP
regulations.  Most process operations at existing metallic mineral
processing plants use dynamic wet scrubbers with a pressure drop of
about 1.5 kPa (6 inches of water) to comply with the SIP requirements.
Therefore, dynamic wet scrubbers at this pressure drop, as presented in
Chapter 4, have been selected as the baseline control device.  This
control device is referred to as Control Option 1.  Fractional efficiency
curves for a 1.5-kPa (6-inch) dynamic scrubber indicate that with the
most adverse expected particle size distribution (x = 1.5 pm) and inlet
concentrations of 2.3 g/DNm3 (1.0 gr/dscf), the achievable emission
level would be 0.35 g/DNm3 (0.15 gr/dscf).
6.3.2  Regulatory Alternative 2
     As explained in Chapter 4, the control efficiency of wet scrubbers
can be increased by raising the pressure drop across the unit.  As a
result, the theoretical number of control options based on wet scrubbers
is unlimited.
     A 3.7-kPa (15-inch) venturi scrubber has been selected to represent
an intermediate level of control between the baseline and the baghouse
                                 6-10

-------
or high energy scrubber control level.  This control unit is Control
Option 2.  Performance evaluations indicate that the 3.7-kPa (15-inch)
scrubber is capable of reducing the worst-case uncontrolled emissions
                                                              3
level (1.0 gr/dscf and particle size x = 1.5 urn) to 0.14 g/DNm
(0.06 gr7dscf).  This intermediate level of control represents Regulatory
Alternative 2.
6.3.3   Regulatory Alternative 3
     The most effective feasible control level option for most conditions
in the metallic mineral industries is a fabric filter which is Control
Option 3a under Regulatory Alternative 3.  Source test data indicate
that a baghouse will reduce the worst-case uncontrolled emissions
(particle size distribution, x = L5 urn) to a controlled level less than
0.046 g/DNm3 (0.02 gr/dscf).
     Because of high moisture conditions, baghouses may not be practical
for all emission points.   A wet scrubber may be used under these
conditions.  Comparison of control efficiency evaluations indicates that
a 7.5-kPa (30-inch) venturi scrubber would equal the performance of the
baghouse under worst-case, high-moisture conditions.  This high energy
scrubber is Control Option 3b under Regulatory Alternative 3.   Therefore,
the most effective control level is represented by an emission limit of
0.046 g/DNm3 (0.02 gr/dscf).
6.3.4  The "Worst-Case Analysis Method"
     Because of the possible confusion with the use of worst-case premises
in the development of the regulatory alternative, the explanation of the
"worst-case analysis method" first presented in Chapters 3 and 4,
deserves repeating here.
     Discussions of worst-case conditions and the design of control
equipment to handle worst-case conditions should not be interpreted as a
recommendation or a requirement that certain types of equipment would be
necessary to meet a specific emission level under all conditions found
in the metallic mineral industries.  The selection of control  equipment
for an actual emissions source requires consideration of the character-
istics of only that source.  Rather, the discussions of worst-case
conditions are based on two premises.  First, if an emission level can
be demonstrated as achievable under worst-case conditions, then it is
                                 6-11

-------
achievable under all conditions found in the industry.   Second,  if the
cost of achieving an emission level is based on the cost of control
equipment designed to meet that emission limit under worst-case
conditions, then the actual cost of control equipment designed to meet
the emission level under less than worst-case conditions should be less.
6.3.5  Control Equipment Options for Each Regulatory Alternative
     For purposes of economic analysis, the design parameters of each
control equipment option for each regulatory alternative have been set.
The 1.5-kPa (6-inch) dynamic scrubber which is the basis for Regulatory
Alternative 1 operates at a liquid to gas ratio of 0.13 L/m  (1 gal./lO ft ).
The 3.7-kPa (15-inch) venturi scrubber which is the basis for
Alternative 2 operates at a liquid to gas ratio of 0.94 L/m  (7 gal.710 ft ).
The 7.5-kPa (30 inches of water) venturi scrubber of Alternative 3b has
a liquid to gas ratio of 1.07 L/m3 (8 gal./103ft3).  The baghouse option
for Alternative 3a  is a pulse jet cleaning type with an air to cloth
ratio of 6 to 1.  The bag fabric is assumed to be Dacron felt and the
unit operates at a  pressure drop of 1.5 kPa (6 inches of water).  All
emissions collected from the baghouse were presumed recycled to the
process at negligible cost.  The control equipment alternatives are
keyed numerically for presentation in the tables.
     •    Control Option 1 - 1.5-kPa  (6-inch W.G.) dynamic scrubber
     •    Control Option 2 - 3.7-kPa  (15-inch W.G.) venturi scrubber
     •    Control Option 3a - 1.5-kPa  (6-inch W.G.) baghouse
     •    Control Option 3b - 7.5-kPa  (30-inch W.G.) venturi scrubber
6.4  MODEL PLANT  PARAMETERS
6.4.1   Introduction
     This  section presents the  parameters  necessary for evaluating the
economic,  energy  and environmental impacts  of  the  regulatory alternatives
for  each model  plant in  each individual  industry.  The process  and
control device  parameters  are  assembled on  the basis of responses  to
Section 114  letters, plant visits, literature  searches, and discussions
with control  equipment manufacturers  (GCA,  1979).  The  following
subsections  (6.4.2  to 6.4.11)  present the  parameters for each  of  the  ten
ore  processing  industries  with expected growth in  processing  capacity.
                                  6-12

-------
Each of the subsections is divided into four sections.   The four sections
present the process units, model plant capacity, capacity independent
model plant parameters, and capacity dependent model plant parameters.
     Each description includes a schematic figure of a model facility
and each emission point associated with the process equipment is
identified.  The grouping of emission points into unit processes is also
presented.
     6.4.1.1  Process Unit.  Associated emission points at each model
plant can be grouped together into one process unit.  Each of these
process units is treated as a single source and can be controlled by one
emission control system.  The economic, energy and environmental impact
analysis of the regulatory alternatives is based on the application of
each control equipment option to each process unit.  In order to determine
the environmental impacts through dispersion analysis, stack and flue
gas parameters from the control device must be specified.  Tables are
provided in each subsection which present the process units and stack
and control system parameters for each model plant and regulatory
alternative.
     6.4.1.2  Model Plant Capacity.  Many economic factors associated
with the industries vary with the production rate.  These "economies
of scale" must be considered in determining the economic impact of the
regulatory options.  Therefore, the range of production capacities found
within each individual industry must be represented by the model plants.
One or more production capacity model plants are presented for each of
the growth industries and are representative of the range of capacities
expected, in the individual industry.  Within each model plant for a
particular industry the particular emission points vary only by size of
equipment and number of parallel processing lines.  The processing
methods presented in the process schematic remain constant throughout
the capacity range.
     6.4.1.3  Capacity Independent Model Plant  Parameters.  Some parameters
selected for comparing the economic and environmental impacts of the
regulatory alternative vary among the various metallic mineral industries,
but are assumed to be constant  in an individual industry across its
                                  6-13

-------
capacity range.  These parameters are operating hours, capacity
utilization rate, growth rate, ore grade processed, and the total  ore
processed.  The values presented for each parameter have been determined
to be representative of the individual metallic mineral processing
industry (GCA, 1979).
     6.4.1.4  Capacity Dependent Model Plant Parameters.  Although some
parameters may be taken as constant, others vary with capacity.  These
parameters include the land required for the plant and the process
energy requirements of the total plant and are provided for each model
plant capacity for each industry.  For costing purposes, it is assumed
that only product recovered from dryer or load out units is of
sufficient quality to be economically recoverable.  Within an individual
industry the process configuration is constant for each model plant;
however, the size and number of each process unit or emission point may
vary at different capacities.  A table is provided in each subsection
that provides the number, size and gas volume associated with each
emission point.  Separate tables are provided in each subsection for the
total plant energy requirements.
                                 6-14

-------
6.4.2  Aluminum Ore Processing Facility
     6.4.2.1  Process Units Description.  Aluminum is produced from
alumina which results when bauxite is processed.  The aluminum model
plants consist of four process units, three associated with bauxite
processing (raw product) and one associated with alumina processing.
The process units are listed below.
     Bauxite ore
     A. Coarse ore storage and reclaim.
     B. Hammer mill and all screens and associated transfer points.
     C. Fine ore bins and associated transfer points.
     Alumina
     D. Product loadout and associated transfer points.
     As noted in Chapter 3, ship loading and unloading and calcining are
not included.  Dockside transfer operations after ship unloading or
before ship loading are covered in this document.
     6.4.2.2  Model Plant Capacity.  Model plant capacities are 140 Mg/hr
(150 tons/hr) and 270 Mg/hr (300 tons/hr) based on the expected process
rate of new plants.
     6.4.2.3  Capacity Independent Model Plant  Parameters.
     9    Hours of operations - 5,820  hours/year.
     »    Capacity Utilization - 91 percent.
     e    New facilities by 1985 - 2.
     9    Bauxite ore grade - 22 percent aluminum.
     6.4.2.4  Capacity Dependent Model  Plant Parameters.
140 Mg/hr (150 tons/hr) Model Plant.
     «    Land Required 126,000 M2 (1,360,000 ft2).*
                                     tjUtjU
     •    Energy  Required 8.04 PJ/yr.
  Includes  only the mineral  processing plant itself without the tailings
  pond areas.   The plant area assumes a rectangular boundary located
  a minimum of 61 meters (200 ft) from the buildings.
 **
   PJ/yr  =  Petajoule  _ 1 x 1015 joules
              year            year
                                  6-15

-------
270 Mg/hr (300 tons/hr) Model Plant.

     t    Land Required 204,000 M2 (2,200,000 ft2)*
                                      A*
     •    Energy Required 16.08 PJ/yr.
 C
 Includes only the mineral processing plant itself without the tailings
 pond areas.  The plant area assumes a rectangular boundary located a
 minimum of 61 meters (200 ft) from the buildings.
PJ/yr = Peta joule
          year
                     =  1 x 1015 joules
                              year
                                 6-16

-------











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6-19

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                    PLANT  (UP TO  140 Mg/hr)
        PLANT (270 Mg/hr)
KEY
o
                            SCALE
EMISSION POINT
CONVEYOR
                                 30.5 m
                                (100 ft)
EMISSION POINT KEY

A - COARSE ORE RECLAIM
B - HAMMERMILL
C - FINE ORE BIN
D - PRODUCT LOADOUT
                 Figure 6-3.  Aluminum model plant plot plans.
                                    6-20

-------
Table 6-4.  ENERGY REQUIREMENTS FOR AN
    ALUMINUM ORE PROCESSING PLANT3
                     Gigajoules  per
                     net megagram of
                     aluminum metal
Million BTU's per
    net ton of
  aluminum metal
Mining
Drilling
Drill bits, drilling machines
Explosives
SUBTOTAL
Shovel loading
Electrical energy
Materials, repair, and maintenance
SUBTOTAL
Truck transportation
Diesel fuel oil
Truck materials, tires, and repair
SUBTOTAL
Crushing, washing, and screening
Crushing and screening electrical
energy
Pumping electrical energy
Machinery wear and service energy
SUBTOTAL
Dry i ng
Transportation
Bayer processing
Crushing and grinding
Electrical energy
Lime
SUBTOTAL
Digestion
Steam
Caustic soda
SUBTOTAL
0.01
0.02
0.03
0.13
0.03
0.16
0.12
0.02
0.14
0.15
0.08
0.02
0.25
2.21
2.77
0.38
1.00
1.38
19.73
5.24
24.97
0.01
0.02
0.03
0.12
0.03
0.15
0.11
0.02
0.13
0.14
0.07
0.02
0.23
2.00
2.51
0.35
0.90
1.25
17.90
__jk75
22.65
              (continued)
                 6-21

-------
                            Table 6-4.   Concluded
                                        Gigajoules  per
                                        net megagram of
                                        aluminum metal
aBattelle, 1975.

bGigajoule = 109 joules.
Million BTU's per
    net ton of
  aluminum metal
Clarification
Electrical energy
Cooling
Electrical energy
Precipitation-f i 1 tration
Electrical energy
Evaporation
Steam
Spent liquor recovery
Electrical energy
Net steam usage
SUBTOTAL
TOTAL
Ore grade
Giga joule per net megagram (ton) of
aluminum ore (bauxite)
0.37
0.07
0.82
11.11
0.89
0.97
1.76
46.05

0.22
10.13
0.34
0.06
0.74
10.08
0.81
0.88
1.69
41.86

0.22
9.21
                                    6-22

-------
6.4.3  Copper Ore Processing Facility
     6.4.3.1  Process Units Description.   The copper model plants consist
of the following process units:
     A.  The primary crushing including the primary crusher, grizzly,
screens, coarse ore storage bins, and transfer points.
     B.  Secondary crushing units including a secondary crusher and
associated screens, ore bins, and transfer points.
     C.  Tertiary crushing units including a tertiary crusher and
associated screens, fine ore bins, and transfer points.
     D.  Fine ore bins if not ducted to a crusher control device.
     E.  The dryer unit including the dryer and associated transfer
points.
     F.  The product loadout unit including all packaging, product bins,
and transfer points.
     6.4.3.2  Model Plant Capacity.  Model plant  sizes are 140 Mg/hr
(150 tons/hr) and 540 Mg/hr (600 tons/hr) based on new plant information.
     6.4.3.3  Capacity Independent Model Plant Parameters.
     •    Hours of Operations  - 8,500 hours/year.
     •    Capacity Utilization - 96 percent.
     «    New facilities by 1985 - 2.
     «    Ore Grade - 0.45 percent.
     6.4.3.4  Capacity Dependent Model Plant Parameters.
140 Mg/hr (150 tons/hr) Model  Plant.
     •    Land Required 126,000 M2 (1,360,000  ft2).*
     •    Energy  Required  0.38 PJ/yr.
540 Mg/hr (600 tons/hr) Model  Plant.
     »    Land Required 364,000 M2 (3,920,000  ft2).*
     «    Energy  Required  1.55 PJ/yr.
  Includes only the mineral  processing plant itself without the tailings
  pond areas.   The plant area assumes a rectangular boundary located a
  minimum of 61 meters (200  ft) from the buildings.
                                  6-23

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     PLANT (UP TO 140 Mg/hr)
     PLANT  (540 Mg/hr)
KEY
O  EMISSION POINT
= CONVEYOR
(D  STOCKPILE

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m C - TERTIARY CRUSHER
ft) D - FINE ORE BINS
                                                     E - DRYER
                                                     F - PRODUCT LOADOUT
                  Figure 6-5.  Copper model plant plot plans.
                                  6-27

-------
Table 6-7.
COPPER
•
Mine
Excavation
Electrical energy
Natural gas
Petroleum fuels (diesel)
Coal
Explosives
SUBTOTAL
Transportation
Waste rock to dumps
(truck-2 miles)
Ore to mill
(electric rail -8 miles)
SUBTOTAL
Concentrator
Crushing
Electrical energy
Grinding
Electrical energy
Steel balls and rods
SUBTOTAL
Flotation
Electrical energy
Natural gas
Petroleum fuels
Steam
Inorganic reagents
Organic reagents
SUBTOTAL
TOTAL
Ore grade
ENERGY REQUIREMENTS FOR A
ORE PROCESSING PLANT9
Gigajoules per
net megagram of
copper metal


9.630
0.257
6.242
\ 0.039
5.607
21.775


2.569

0.982
3.551


4.840

24. 588
5.555
34.983

6.678
2.867
0.282
0.596
3.151
0.663
14. 237
74.546

0.0045
Gigajoule per net megagram (ton) of
copper ore
0.334

Million BTU's per
net ton of
copper metal


8.735
0.233
5.662
0.035
4.904
19.569


2.330

0.891
3.221


4.390

22.302
5.039
31.731

6.057
2.600
0.256
0.541
2.858
0.601
12.914
67.435

0.0045

0.303
 Battelle, 1975.
bGigajoule = I09 joules.
                                    6-28

-------
6.4.4  Gold Ore Processing Facility
     6.4.4.1  Process Units Description.  The gold model plants consist
of the following process units:
     A.  Primary crushing unit including the primary crusher and
associated dumping station, grizzly, screens, coarse ore storage bins,
and transfer points.
     B.  Secondary crushing units including a secondary crusher and
associated screens, ore bins, and transfer points.
     C.  Fine ore bins.
     Because of the small quantities and characteristics of the final
product, product loading operations are not covered on this document.
     6.4.4.2  Model Plant Capacity.  Model plant sizes are 68 Mg/hr
(75 tons/hr) and 140 Mg/hr (150 tons/hr) based on new plant information.
     6.4.4.3  Capacity Independent Model Plant Parameters.
     •    Hours of Operation - 5,820 hours/year.
     •    Capacity Utilization - 95 percent.
     e    New facilities by 1985 - 2.
     •    Ore Grade - 0.00063 percent.
     6.4.4.4  Capacity Dependent Model Plant Parameters.
68 Mg/hr (75 tons/hr) Model Plant.
     0
     •    Energy Required 0.21 PJ/yr.
140 Mg/hr (150 tons/hr) Model Plant.
     •    Land Required 126,000 M2 (1,360,000 ft^).;
     •    Energy Required 0.42 PJ/yr.
          Land Required 126,000 M2 (1,360,000 ft2).*
                                                2*
*Includes only the mineral processing plant itself without the tailings
 pond areas.   The plant area assumes a rectangular boundary located a
 minimum of 61 meters (200 ft) from the buildings.
                                 6-29

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-------
           PLANT (UP TO 140 Mg/hr)
 KEY
 O  EMISSION  POINT
= CONVEYOR
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  SCALE
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(100 ft)
EMISSION ...POINT KEY
A.- PRIMARY CRUSHER
B - SECONDARY CRUSHER
C - FINE ORE BIN
                     Figure 6-7.   Gold model  plant plot plans.
                                     6-33*.

-------
Table 6-10.  ENERGY REQUIREMENTS FOR A
      GOLD ORE PROCESSING PLANTS*
                     Gigjoules  per
                     net megagram of
                        gold metal
Million BTU's per
   net ton of
   gold metal
Open pit mining
Explosives
Gasoline
Diesel fuel oil
Lubricants
SUBTOTAL
Crushing and grinding
Electrical energy
Liners
Steel balls
SUBTOTAL
Leaching
Electrical energy
Diesel fule oil
Chlorine
Chlorine transportation
(300 miles by rail)
Sodium cyanide
Cyanide tranportation
(300 miles by rail)
Soda ash (natural)
Soda ash transportation
(500 miles by rail)
SUBTOTAL
Thickening
Electrical energy
Lime
Lime transportation
(50 miles by truck)
Additives
SUBTOTAL

9,182
2,326
21,581
1,103
34,192

16,840
2,059
168
19,067

3,645
6,999
4,862

49
632

4
309
1
13
16,513

4,035
. 5,189

73
61
9,358

8,328
2,110
19,575
1,000
31,013

15,274
1,868
152
17,294

3,306
6,348
4,410

44
573

4
280

12
14,977

3,660
4,707

66
55
8,488 .
              (continued)
                 6-34

-------
                          Table 6-10.  Concluded
                                                b
                                       Gigjoules  per
                                       net megagram of
                                          gold metal
     Ore grade

     Gigjoule per net megagram (ton) of
       gold ore        ,  ,
6.0 x 10


 0.530
                                                     -6
              Million BTU's per
                  net ton of
                  gold metal
Clarification and precipitation
Electrical energy
Zinc
Zinc tranportation
(500 miles by rail)
Filter aid
Filter aid transportation
(500 miles by rail)
SUBTOTAL
Fluxing, melting and casting
Electrical energy,
Diesel fuel oil
Flux
SUBTOTAL
Pumping tailing and, water
Reclamation
Electrical energy
TOTAL
3,272
831

4
2,224

19
6,350
172
1,069
1
1,242


830
87,552

2,968
754


2,017
1 "7
17
5,760
156
970
1
1,127


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79,412

6.0 x 10


  0.480
                            -6
aBattelle, 1976.

bGigajoule = 109 joules.
                                    6-35

-------
6.4.5  Iron Ore Processing Facility
     6.4.5.1  Process Units Description.  The model plants for the iron
ore processing industry consists of the following process units:
     A.  The primary crushing unit including the primary crusher and
associated dumping station, grizzly, screens, coarse ore storage bins,
and transfer points.
     B.  Secondary crushing units including a secondary crusher and
associated screens, fine ore bins, and transfer points.
     C.  Tertiary crushing units including tertiary crusher and
associated screens, fine ore bins, and transfer points.
     D.  The fine ore bins if not ducted to a crusher control device.
     E.  The prpduct loadout unit including all packaging, product bins,
transfer points, and loadout mechanisms before entry holds.
     As noted in Chapter 3, emissions from pelletizing furnaces are not
covered in this document.
     6.4.5.2  Model Plant Capacity.  Two new iron ore processing plants
are projected between now and 1985, one at 1,100 Mg/hr (1,200 tons/hr)
and one at 2,200 Mg/hr (2,400 tons/hr).
     6.4.5.3  Capacity Independent Model Plant Parameters.
     •    Hours of operation - 8,500 hours/year.
     •    Capacity Utilization - 90 percent.
     •    New facilities by 1985 - 2.
     •    Ore grade - 36 percent.
     6.4.5.4  Capacity Dependent Model Plant Parameters.
1,100 Mg/hr (1,200 tons/hr) Model Plant
     •    Land Required 364,000 M2 (3,920,000 ft2).*
     •    Energy Required 1.41 PJ/yr.
2,200 Mg/hr (2,400 tons/hr) Model Plant.
     •    Land Required 490,000 M2 (5,270,000 ft2).*
     •    Energy Required 2.82 PJ/yr.
^Includes only the mineral processing plant itself without the tailings
 pond areas.  The plant area assumes a rectangular boundary located a
 minimum of 61 meters (200 ft) from the buildings.
                                 6-36

-------


















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6-39

-------
    PLANT (1100 Mg/hr')
                                      '2

                                      '3

                                      '4
     PLANT (2200 Mg/hr)
KEY
Q  EMISSION POINT
= CONVEYOR
©  STOCKPILE
  SCALE
 30.5 m
(100 ft)
EMISSION POINT KEY
A - PRIMARY CRUSHER
B - SECONDARY CRUSHER
C - TERTIARY CRUSHER
D - FINE ORE BINS
E - PRODUCT LOADOUT
                     Figure 6-9.   Iron model  plant plot, plans.
                                   6-40

-------
      Table 6-13.   ENERGY REQUIREMENTS FOR AN IRON ORE PROCESSING PLANT
                                        Megajoule  per
                                        net megagram of
                                            iron ore
                1,000 BTU's per
                  net ton of
                   iron ore
Consumption
  Crushing
  Concentration

     TOTAL
  6.47
145.86

152.33
  5.87
132.30

138.17
aMegajoule equals 10  joules.

(114 Questionnaire response)
                                    6-41

-------
6.4.6  Lead/Zinc Ore Processing Facility
     6.4.6.1  Process Units Description.  The model plants for the
lead/zinc ore processing industry consist of the following process
units:
     A.  The primary crushing unit including the primary crusher and
associated dumping station, grizzly, screens, coarse ore storage bins,
and transfer points.
     B.  Secondary crushing units including a secondary crusher and
associated screens, ore bins, and transfer points.
     C.  Tertiary crushing units including a tertiary crusher and
associated screens, fine ore bins and transfer points.
     D.  The fine ore bins if not ducted to a crusher control device.
     E.  The dryer unit including the dryer and associated transfer
points.
     F.  The product loadout unit including all packaging,product bins,
transfer points, and loadout mechanisms.
     6.4.6.2  Model Plant Capacity.  Three new lead/zinc ore processing
plants are projected between now and 1985, one at 540 Mg/hr (600 tons/hr)
and two at 270 Mg/hr (300 tons/hr).
     6.4.6.3  Capacity Independent Model Plant Parameters.
     •    Hours of operation - 5,820 hours/year.
     *    Capacity Utilization - 87 percent.
     •    New facilities by 1985 - 3.
     •    Ore grade - 4.5 percent lead and 1 percent zinc.
     6.4.6.4  Capacity Dependent Model Plant Parameters.
270 Mg/hr (300 ton/hr) Model Plant.
     •    Land Required 204,000 M2 (2,200,000 ft2).*
     •    Energy Required 1.51 PJ/yr.
540 Mg/yr (600 tons/hr) Model Plant.
     •    Land Required 364,000 M2 (3,920,000 ft2).*
     •    Energy Required 3.02 PJ/yr.
 Includes only the mineral processing plant itself without the tailings
 pond areas.  The plant area assumes a rectangular boundary located a
 minimum of 61 meters (200 ft) from the buildings.
                                 6-42

-------
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-------
    PLANT  (270 Mg/hr)
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KEY
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= CONVEYOR
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EMISSION POINT KEY
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B - SECONDARY CRUSHER
C - TERTIARY CRUSHER
D - FINE ORE BINS
E - DRYER
F - PRODUCT LOADOUT
               Figure 6-11.  Lead/Zinc model plant plot plans.
                                    6-46 n

-------
                   Table 6-16.   ENERGY REQUIREMENTS FOR A
                       LEAD/ZINC ORE PROCESSING PLANT3
Giga joules per
net megagram of
lead/zinc metal
Mining
Steel
Explosives
Electrical energy
Diesel fuel oil
Gasoline
SUBTOTAL
Crushing
Electrical energy
Grinding and classifying
Electrical energy
Steel
SUBTOTAL
Beneficiation
Conditioning and flotation
Thickening and filtering
Organic reagents
Inorganic reagents
Miscellaneous
SUBTOTAL
Rail transportation
Dry i ng
Electrical energy
TOTAL
Ore grade
Gigajoule per net megagram (ton) of
lead/zinc ore
0.347
0.503
4.102
1.089
0.079
6.121
0.240
3.652
0.583
4.475
1.335
0.174
0.062
0.227
OJ360
1.858
1.130
0.023
13.63
0.07
0.954
Million BTU's per
net ton of
lead/zinc metal
0.315
0.456
3.721
0.988
0.072
5.552
0.218
3.312
0.529
4.059
' 1. 211
0.158
0.056
0.206
0.054
1. 685
1.025
0.021
12.36
0. 07
0.865
aBattelle, 1975.
bGigajoule = 109 joules.
                                    6-47

-------
6.4.7  Molybdenum Ore Processing Facility
     6.4.7.1  Process Units Description.  The model plants for the
molybdenum ore processing industry consist of the following process
units:
     A.  The primary crusher unit including the primary crushing unit
including the primary crusher and associated dumping station, grizzly,
screens, coarse ore storage bins, and transfer points.
     B.  Secondary crushing units including a secondary crusher and
associated screens, ore bins, and transfer points.
     C.  Tertiary crushing units including a tertiary crusher and
associated screens, fine ore bins, and transfer points.
     D.  The fine ore bins if not ducted to a crusher control device.
     E.  The dryer unit including the dryer and associated transfer
points.
     F.  The product loadout units including all packaging product bins,
transfer points, and loadout mechanisms.
     6.4.7.2  Model Plant Capacity.  Three new molybdenum ore processing
plants are projected between now and 1985, one at 270 Mg/hr  (300 tons/hr)
and two at 1,100 Mg/hr (1,200 tons/hr).
     6.4.7.3  Capacity Independent Model Plant Parameters.
     •    Hours of Operation - 8,500 hours/year.
     •    Capacity Utilization - 84 percent.
     •    New facilities by 1985 - 3.
     •    Ore grade - 0.4 percent.
     6.4.7.4  Capacity Dependent Model  Plant Parameters.
270 Mg/hr (300 tons/hr) Model Plant.
     •    Land Required 204,000 M2 (2,200,000 ft2).*
     •    Energy Required 1.53 PJ/yr.
1,100 Mg/hr (1,200 tons/hr) Model  Plant.
     •    Land Required 364,000 M2 (3,920,000 ft2).*
     •    Energy Required 6.12 PJ/yr.
 ^Includes  only the mineral  processing plant itself without  the  tailings
  pond areas.   The  plant area assumes  a rectangular boundary located  a
  minimum of 61 meters  (200  ft)  from the buildings.
                                  6-48

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    PLANT (270 Mg/hr)
     PLANT  (1100 Mg/hr)
KEY
     EMISSION POINT
     CONVEYOR
     STOCKPILE
  SCALE


 30.5 m
(100 ft)
EMISSION POINT KEY
A - PRIMARY CRUSHER
B - SECONDARY CRUSHER
C - TERTIARY CRUSHER
D - FINE ORE BINS
E - DRYER -
F - PRODUCT LOADOUT
           Figure 6-13.  Molybdenum model plant plot plans,
                                   6-52

-------
                    Table 6-19.   ENERGY REQUIREMENTS FOR
                      MOLYBDENUM ORE PROCESSING PLANT*
                                        Gigajoules  per
                                        net megagram of
                                        molybdenum metal
               Million BTU's per
                  net ton  of
               molybdenum  metal
Mining
  Electrical energy
  Natural gas
  Liquid hydrocarbons
  Explosives
     SUBTOTAL

Concentration
  Crushing
  Grinding
  Flotation
  Other electrical energy
    (e.g. tailings disposal, water
    pumping, etc.)
  Inorganic reagents
  Organic reagents
  Steel for grinding
     SUBTOTAL

General plant energy

     TOTAL

     Ore grade

     Gigajoule per net megagram (ton) of
       molybdenum ore
 21.54
 24.53
  8.17
  3.32
 57.56
  5.90
 37.01
 17.39
 16.33
  7.03
  4.09
  7.69
 95.44

  9.91

162.92


 0.004


 0.662
 19.54
 22.25
  7.41
  3.01

 52.21
  5.35
 33.57
 15.77
 14.81
  6.38
  3.71
  6.98
 86.57

  8.99

147.77


 0.004


 0.600
aBattelle, 1976.
bGigajoule = 10  joules.
                                    6-53

-------
6.4.8     Silver Ore Processing Facility
     6.4.8.1  Process Units Description.  The model plants for the
silver ore processing industry consist of the following process units:
     A.  The primary crusher unit including the primary crusher and
associated dumping station, grizzly, screens, coarse ore storage bins,
and transfer points.
     B.  Secondary crushing units including a secondary crusher and
associated screens, ore bins, and transfer points.
     C.  Tertiary crushing units including a tertiary crusher and
associated screens, fine ore bins, and transfer points.
     D.  Fine ore bins.
     Because of the small quantities and characteristics of the final
product, product loading operations are not covered in this document.
     6.4.8.2  Model Plant Capacity.  Three new silver ore processing
plants are projected between now and 1985, two at 45 Mg/hr (50 tons/hr)
and one at 140 Mg/hr (150 tons/hr).
     6.4.8.3  Capacity Independent Model Plant Parameters.
     «    Hours of operation - 5,820 hours/year.
     •    Capacity Utilization  - 90 percent.
     •    New facilities by 1985 - 3.
     •    Ore grade - 0.015 percent.
     6.4.8.4  Capacity Dependent Model  Plant  Parameters.
45 Mg/hr (50 tons/hr) Model Plant.
     •    Land  Required  126,000 M2  (1,360,000 ft2).*
     •    Energy Required 0.095 PJ/yr.
140 Mg/hr (150  tons/hr)  Model  Plant.
     •    Land  Required  126,000 M2  (1,360,000 ft2).*
     •    Energy Required  0.285 PJ/yr.
  Includes only the mineral  processing plant itself without the tailings
  pond areas.   The plant area assumes a rectangular boundary located a
  minimum of 61 meters (200 ft) from the buildings.
                                  6-54

-------
















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 Figure 6-15.  Silver model plant plot plans.
                    6-.5B

-------
     Table 6-22.  ENERGY REQUIREMENTS FOR SILVER ORE PROCESSING PLANTS'
                                        Gigajoules  per
                                        net megagram of
                                          silver bars
     Ore grade

     Gigajoule per net megagram (ton) of
       silver ore
0.00015


 0,359
                Million BTU's
                  net ton of
                  silver bars
0.00015


 0.326
          per
Underground mining, crushing, grinding,
and concentrating
Electrical energy
Diesel fuel oil
Gasoline
LP gas
Oxygen
Lubricants
Explosives
Lime
Steel shapes
Soda ash (synthetic)
Xanthates
Transportation
SUBTOTAL
Leaching and thickening
Electrical energy
Distillate fuel oil
Sodium cyanide
Soda ash (synthetic)
Lime
Additives
SUBTOTAL
Clarification and precipitation
Electrical energy
Zinc
Filter aid
SUBTOTAL
TOTAL
1,405.0
202.5
12.2
32.0
0.1
8.8
78.2
3.2
62.6
30.2
8.5
0.6
1,843.9
153.6
140.0
14.0
13.9
103.9
1.4
426.8
65.5
16.6
46.5
128.6
2,393.9

1,274.4
183.7
11.1
29.0
0.1
8.0
70.9
2.9
56.8
27.4
7.7
0.5
1,672.5
139.3
127.0
12.7
. 12.6
94.2
1.3
387.1
59.4
15.1
42.2
116.7
2,176.3

Mattel le, 1976.

 Gigajoule = 10  joules.
                                     6-59

-------
6.4.9  Titanium/Zirconium Sand Type Ore Processing Facility
     6.4.9.1  Process Units Description.  The model plants for the
titanium/zirconium sand type ore processing industry consists of the
following process units:
     A.  The dryer unit including the dryer and associated transfer
points.
     B.  The product loadout including all product bins, transfer points,
and loadout mechanisms.
     As noted in Chapter 3, calcining operations are not included.
     6.4.9.2  Model Plant Capacity.  Titanium/zirconium sand type ore
processing capacity is expected to increase as a result of a 270 Mg/hr
(300 ton/hr) expansion and a new 540 Mg/hr (600 ton/hr) plant.
     6.4.9.3  Capacity Independent Model Plant Parameters.
     •    Hours of operation - 8,500 hr/yr.
     •    Capacity utilization - 90 percent.
     •    New facilities by 1985 - 1.
     •    Expansions by 1985 - 1.
     •    Ore grade - 1.5 percent Ti02
                       0.9 percent Zirconium
     6.4.9.4  Capacity Dependent Model Plant Parameters.
270 Mg/hr (300 tons/yr) Model Plant
     •    Land Required - 108,000 M2 (1,160,000 ft2)*
     0    Energy Required - 0.10 PJ/yr
540 Mg/hr (600 tons/hr) Model Plant
     •    Land Required - 204,000 M2 (2,200,000 ft2)*
     •    Energy Required - 0.22 PJ/yr
 Includes only the mineral processing plant itself without the tailings
 pond areas.   The plant area assumes a rectangular boundary located
 a minimum of 61 meters (200 ft) from the buildings.
                                 6-60

-------













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PLANT (270 Mg/hr)
               Classification
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                                               JEL
PLANT (540 Mg/hr)
      Classification
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                                                        (A)
 KEY
    EMISSION POINT

    CONVEYOR
                            SCALE:
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 30.5 m

(100 ft)
Figure 6-17.  Titanium/Zirconium sand type ore model plant plot plans.

                                  6-64

-------
6.4.10    Tungsten Ore Processing Facility
     6.4.10.1  Process Units Description.  The model plants for the
tungsten ore processing industry consist of the following process units:
     A.  The primary crushing unit including the primary crusher and
associated dumping station, grizzly, screens, coarse ore storage bins,
and transfer points.
     B.  Secondary crushing units including a secondary crusher, and
associated screens, ore bins, and transfer points.
     C.  Tertiary crushing units .including a tertiary crusher, and
associated screens, fine ore bins, and transfer points.
     D.  Fine ore bins when not directed to a crusher control device.
     E.  The dryer unit including the dryer and associated transfer
points.
     F.  The product loadout unit including all packaging, product bins,
transfer points, and loadout mechanisms.
     6.4.10.2  Model  Plant Capacity.  Tungsten ore processing capacity
is expected to increase as a result of a new 23 Mg/hr (25 ton/hr) plant.
     6.4.10.3  Capacity Independent Model Plant Parameters.
     9    Hours of operation - 5,820 hours/year.
     •    Capacity utilization - 90 percent.
     e    New facilities by 1985 - 1.
     •    Ore grade - 0.5 percent.
     6.4.10.4  Capacity Dependent Model Plant Parameters.
23 Mg/yr (25 tons/hr) Model Plant.
     •    Land Required 126,000 M2 (1,360,000 ft2).*
     «    Energy Required 0.16 PJ/yr.
 Includes only the mineral processing plant itself without the tailings
 pond areas.  The plant area assumes a rectangular boundary located a
 minimum of 61 meters (200 ft) from the buildings.
                                 6-65

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                      PLANT(23 Mg/hr)
KEY:
O
EMISSION POINT
CONVEYOR
STOCKPILE
 SCALE:
 30.5 m
(100 ft)
EMISSION POINT KEY
A - PRIMARY CRUSHER
B - SECONDARY CRUSHER
C - TERTIARY CRUSHER
D - FINE ORE BIN
E - DRYER
F - PRODUCT LOADOUT
               Figure 6-19.   Tungsten model plant plot plans.
                                   6-69

-------
     Table 6-27.  ENERGY REQUIREMENTS FOR TUNGSTEN ORE PROCESSING PLANT0
                                        Gigajoules  per
                                        net megagram of
                                        tungsten metal
aBattelle, 1976.
bGigajoule = 109 joules.
Million BTU's per
  net ton of
 tungsten metal
Mining, crushing, and grinding
Diesel fuel oil
Gasoline
Explosives
Steel balls and rods, drill bits
SUBTOTAL
Concentration, gravity and flotation
Electrical energy
Soda ash (natural)
Caustic soda
Copper sulfate
Lime
Sodium silicate
Sodium cyanide
Organic reagents
Reagent transportation
SUBTOTAL
Concentration, hydrometallurgical
Electrical energy
Natural gas
Hydrochloric acid
Hydrochloric acid transportation
(200 miles by rail)
Caustic soda
Caustic soda transportation
(200 miles by rail)
SUBTOTAL
Transportation of concentrate
(1,170 miles by rail)
(4,100 miles by water)
SUBTOTAL
TOTAL
Ore grade
Gigajoule per net megagram (ton) of
tungsten ore

123.03
1.03
7.19
12.48
143.73

21.06
2.25
1.92
1.93
1.04
0.84
1.66
3.90
0.12
34.72

1.17
13.48
33.77
0.49

10.82
0.04

59.77

1.69
2.20
3.89
242.11

0.005

1.21

111.6
0.93
6.52
11.32
130.37

19.1
2.04
1.74
1.75
0.94
0.76
1.51
3.54
0.11
31.49

1.06
12.23
30.63
0.44

9.81
0.04

54.21

1.53
2.00
3.53
219.60

0.005

1. 10
                                      6-70

-------
6.4.11  Uranium Ore Processing Facility
     6.4.11.1  Process Units Description.   The uranium model plants
consist of the following process units:
     A.  The primary crushing unit including the primary crusher and
associated dumping station, grizzly, screens, coarse ore storage bins,
and transfer points.
     B.  The fine ore bins.
     Because of the possible hazards associated with radioactive emissions,
the emissions from uranium process dryers and from the handling of
uranium processing product (yellowcake) will be evaluated by the Office
of Radiation Programs and, if appropriate, covered by a National Emission
Standard for Hazardous Air Pollutants (NESHAP) for radionuclides.
     6.4.11.2  Model Plant Capacity.  New model plant capacity in the
uranium industry is expected to include two 23 Mg/hr (25 ton/hr) plants
and three 68 Mg/hr (75 tons/hr) plants.
     6.4.11.3  Capacity Independent Model  Plant Parameters.
     a    Hours of operation - 5,820 hours/year.
     •    Capacity utilization - 95 percent.
     9    New facilities by 1985 - 5.
     e    Ore grade - 0.13 percent uranium.
     6.4.11.4  Capacity Dependent Model Plant Parameters.
23 Mg/hr (25 tons/hr) Model Plant.
     e    Land Required 81,700 M2 (880,000 ft2).*
     ©    Energy Required 0.17 PJ/yr.**
68 Mg/hr (75 ton/hr) Model Plant.
     8    Land Required 590,000 M2 (6,400,000 ft2).*
     ®    Energy Required 0.51 PJ/yr.**
  Includes only the mineral processing plant itself without the tailings
  pond areas.  The plant area assumes a rectangular boundary located a
  minimum of 61 meters (200 ft) from the buildings.
  k
  Klemenic, 1979.
                                 6-71

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                    PLANT (UP TO 68  Mg/hr)
KEY:
o
EMISSION POINT
CONVEYOR
 SCALE:
 30.5 m
(100 ft)
EMISSION POINT KEY
A - PRIMARY CRUSHER
B - FINE ORE BINS
                Figure  6-21.   Uranium model  plant  plot  plans.
                                  6-75

-------
6.5  REFERENCES FOR CHAPTER 6

Battelle Columbus Laboratories, 1975.  Energy Use Patterns in
     Metallurgical and Nonmetallic Mineral Processing (Phase 4 - Energy
     Data and Flowsheets, High-Priority Commodities) Report compiled for
     U.S. Bureau of Mines, U.S. Department of Commerce.  National
     Technical Information Service PB-245 759.  179 p.

Battelle Columbus Laboratories, 1976.  Energy Use Patterns in
     Metallurgical and Nonmetallic Mineral Processing (Phase 6 - Energy
     Delta and Flowsheets, Low-Priority Commodities) Report compiled for
     U.S. Bureau of Mines, U.S. Department of Commerce.  National
     Technical Information Service PB-261 150.  257 p.

Klemenic, John, 1979.  Uranium Production Capability in the United States.
     Report compiled for U.S. Department of Energy.  October, 1979.  10 p.
                                  6-76

-------
     Table 7-2 shows the annual allowable emission rates for the three
regulatory alternative systems and the emission reduction impact for
each segment of the metallic mineral processing industry for the year
1985.  The incremental nationwide emission reduction impact from applying
either Regulatory Alternatives 2 or 3 as opposed to the baseline alterna-
tive (Regulatory Alternative 1) is shown as the bottom line in Table 7-2.
Table 7-2 shows that Regulatory Alternative 3 provides the highest level
of control, reducing total particulate emissions from the metallic
mineral industry by approximately 11,800 Mg (13,000 tons) per year by
1985.
     Because the particulate matter emitted from lead ore processors
would be expected to contain various amounts of lead, an additional
concern for lead ore processors is the maintenance of the National
Ambient Air Quality Standard (NAAQS) for lead in the vicinity of these
plants.  In the absence of a New Source Performance Standard (NSPS) for
metallic mineral plants and also when considering fugitive sources, new
lead ore processing facilities may be required to meet more stringent
emission levels than indicated by typical State standards for generic
particulate matter.  Therefore, the reduction in particulate matter due
to the implementation of an NSPS applicable to lead ore processing plant
may be less than indicated in Table 7-2 because of a higher level of
baseline control required to meet the lead NAAQS.
7.1.2  Dispersion Analysis
     Ground-level particulate matter concentrations at specified locations
downwind from eight model metallic mineral processing plants have been
estimated using atmospheric dispersion modelling (Summerhays, 1981).
Dispersion analyses were based on the Industrial Source Complex (ISC)
model (Bowers et al., 1979).  The ISC model is an expanded version of
the single source CRSTER model, modified to account for aerodynamic
downwash and a larger number of sources and receptors.
     The ISC modelling exercises were based on the model plant
characteristics (stack dimensions, plant configurations, and stack gas
flow characteristics) presented in Chapter 6.  Meteorological data
(temperature, air mass stability, wind speed, and direction) were taken
from weather stations located in areas of the country in which new
metallic mineral plants are expected.  The only terrain effects included

                                 7-3

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in the modelling were those implicitly contained in the meteorological
data.   All receptors were assumed to be at the same elevation as the
plant.  If any of these plants are located in a valley or at a lower
elevation than the surrounding terrain, the concentrations at ground
level  could be significantly higher than those estimated.
     Tables 7-3 through 7-5 present the maximum annual average
concentrations for specified points at various distances downwind from
plants emitting particulate matter at the rates prescribed by the regu-
latory alternatives.  For all plants modelled the highest concentrations
occur at the plant boundary for all three regulatory alternatives.  The
                                                3
plant boundary concentrations range from 33 ug/m  for a uranium plant to
        o
182 ug/m  for a large iron ore plant.  The corresponding values for
                                    o            3
Regulatory Alternative 2 are 13 ug/m  and 73 ug/m .  The values for
                                          3           3
Regulatory Alternative 3 range from 4 ug/m  to 24 ug/m .  As a point of
comparison, the maximum average annual concentration allowed by the
                                                                        o
National Ambient Air Quality Standards for particulate matter is 75 ug/m .
     Tables 7-6 through 7-8 present the highest second-highest 24-hour
average concentrations and the distances from the plant boundary at
which these occur.  The second-highest 24-hour averages are presented
                                  S
because the corresponding National Ambient Air Quality Standard for
                            q
particulate matter (150 ug/m  as a 24-hour average concentration) may be
exceeded only once a year.  The maximum second-highest value occurred at
the plant boundaries for all plants except the small iron ore plants
where it occurred 100 meters (328 feet) outside the boundary.  The
                                           o
24-hour concentrations ranged from 153 ug/m  for uranium plants to
1,007 ug/m3 for large iron ore plants operating under Regulatory Alter-
native 1.  The corresponding values for Regulatory Alternative 2 are
61 jag/1"3 and 403 ug/m3, and the values for Regulatory Alternative 3
                   3            3
ranged from 20 pg/m  to 134 ug/m .
7.2  WATER POLLUTION IMPACT
     Two control systems most often used by the metallic mineral processing
industry to control particulate emissions are fabric filters and wet
scrubbers.  The application of a fabric filter or electrostatic precipi-
tator control system (dry emission-reduction systems) will not have any
                                 7-5

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water pollution impact.  The disposal of water-borne particles collected
in wet scrubbers, however, must be considered.
     Milling wastewater handling practices vary throughout the industry.
There has been a significant trend toward recycling of process water,
particularly in water-limited areas.  The combination of water recycling
and evaporation enables many plants in arid areas to process ore with no
discharge of wastewater.  At these plants, wet scrubber slurries are
typically added to the wet milling operations in order to supplement the
water requirements of these operations.  Thus, there would be no water/
solid waste impact from operations in arid regions using wet scrubbers.
     At other operations, excess mine water, rainfall, or the build up
of interfering compounds may require the discharge of excess water from
the system.  In most of these operations, the wet scrubber slurries can
be processed through the wet milling operations, thus eliminating direct
water/solid waste impact.
     In cases where the direct discharge of wet scrubber slurries to
tailings ponds is required, the impact of these additional discharges on
the total discharge requirements of mine/mill operations was analyzed.
The total mine/mill water usage requirements were abstracted from a
development document for proposed effluent guidelines for the ore mining
and processing industry (Environmental Protection Agency, 1980).  This
document provided daily water discharge volumes for specific existing
and projected new plants for each segment of the metallic mineral
processing industries.
     The total plant water usage shown in Table 7-9 was generated by
performing a linear regression of actual data on plant size and the
corresponding daily water discharge  volume.  After determining the
linear regression equation, the model plant sizes were substituted into
the equation to determine their daily water discharge.  The control
equipment water usage  quantities were estimated assuming the recycling
of water through the control device  with the scrubbing liquid disposed
of as a slurry containing 5 percent  solids.  Thus, for every 5 kilograms
of dust collected, 95  kilograms (95  liters) of water were used.
     Table 7-9 shows the  industry water discharge rates and the
incremental water usage due to the  use of 1.5-, 3.7-, or 7.5-kPa (6-,  15-,
                                  7-12

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or 30-inch) wet scrubbers to meet the requirements of Regulatory
Alternatives 1, 2, and 3, respectively.   The percentage increase in
water discharge due to wet scrubbers for most plants is small,  usually
less than 1 percent.  There is little difference in the water impacts  of
the three regulatory alternatives from the use of wet scrubbers.
     In the case of small tungsten plants, the comparison between mill
discharges and wet scrubber discharges is somewhat biased because most
small plants surveyed in the document cited above are located in arid
regions of country where mine/mill water discharges are small because  of
recycling.  In these cases it is expected that a combination of recycling
of scrubber water through the milling process and the increased use of
baghouses would significantly reduce the wastewater impacts of Regulatory
Alternative 3 to less than those cited in Table 7-9.
7.3  SOLID WASTE DISPOSAL IMPACT
     Compliance with New Source Performance Standards and the subsequent
reduction of particulate emissions will lead to increased production of
solid waste by the emission reduction systems.  The quantities of solid
waste that could be produced by new facilities in each industry segment
are equal to the incremental reduction in particulate emissions with
Regulatory Alternatives 2 and 3.  These quantities are listed in Table 7-2
for the three regulatory alternatives.  The total increase in solid
waste for the metallic minerals industry if Regulatory Alternative 3 is
employed would be approximately 11,800 Mg (13,000 tons) in 1985.
     Most, metallic mineral processing facilities are currently recycling
the solid waste from dry collectors back into the process because the
collected particles are primarily ore or process concentrates.  Slurries
produced by wet collectors are also recycled back to the process, or
conveyed to a tailings pond where the solid particles are separated by
gravity.  Any increase in the production of solid wastes from the appli-
cation of emission control techniques will be insignificant by com-
parison with the amount of tailings produced in the beneficiation of
metallic minerals.  A comparison of control equipment and beneficiation
solid waste production was made using iron ore and  bauxite as worst-case
examples because less tailings are produced per unit of ore processed
                                 7-14

-------
than with other metallic ores.  This comparison indicates that wet
scrubber and baghouse wastes, under worst-case conditions, would be less
than 1.0 percent of the beneficiation tailings.
7.4  ENERGY IMPACT
     The potential energy impact of a regulatory alternative is dependent
on the particular control equipment option used to meet the emission
level.  In comparison with a 1.5-kPa (6-inch) pressure drop wet scrubber
(baseline), a 1.5-kPa (6-inch) pressure drop baghouse (control Option 3a)
will usually use less energy for a given air flow rate.  This energy
savings occurs because baghouses typically use more efficient fans than
wet scrubbers and because baghouses require no energy consumption
associated with the pumping of scrubber liquid.  Therefore the universal
application of baghouses to meet the requirements of Regulatory
Alternative 3 would actually cause a decrease in energy consumption from
present conditions.
     On the other hand the energy consumption from high energy (7.5-kPa
(30-inch)) wet scrubbers can be two to three times the energy consumption
of low energy (1.5-kPa (6-inch)) wet scrubbers.  The application of a
high energy wet scrubber to control emissions from all points in the
model plants surveyed would increase energy consumption from 0.04 percent
for aluminum ore plants to 7 percent for titanium/zirconium ore plants.
This increase is based on a comparison of total plant energy consumption
(excluding calcining and pelletizing) with current control equipment
(1.5-kPa (6-inch) wet scrubbers) and total plant energy consumption with
7.5-kPa (30-inch) wet scrubbers.   Total plant energy consumption was
listed in Chapter 6.  The increase in energy consumption for all
industries with the use of 3.75-kPa (15-inch) wet scrubbers would be
75 terajoules (TJ) per year.  The increase in energy consumption for all
industries with the use of 7.5-kPa (30-inch) wet scrubbers would be
317 TJ per year.  These impacts for Regulatory Alternative 3b are
worst-case projections from the standpoint of control equipment energy
use because it is extremely unlikely that all plants will use only
30-inch pressure drop scrubbers.  Rather, it is likely that most instal-
lations will include baghouses for unit processes without moisture
                                 7-15

-------
concerns and wet scrubbers (often with less than 30-inch pressure drop)
for unit processes with moisture concerns.  Table 7-10 provides the
process and control equipment energy requirements for the model plants
under consideration.  Control equipment energy requirements for a specific
regulatory alternative are calculated on the assumption that one
particular control option is applied to all process units in the model
plant.
7.5  NOISE IMPACT
     When compared with the noise resulting from the operation of ore
crushing and grinding equipment, any additional noise from properly
designed exhaust fans for the control system will be insignificant.  No
significant increase in noise levels over those existing under baseline
control is expected with Regulatory Alternatives 2 or 3.
7.6  OTHER ENVIRONMENTAL CONCERNS
7.6.1  Irreversible and Irretrievable Commitment of Natural Resources
     The alternative control systems will require the installation of
additional equipment, regardless of which alternative emission control
system is selected.  This will require the additional use of steel and
other resources.  This commitment of resources will be  small compared
with the national usage of each resource.  There are expected  to be no
significant amounts of space (or land) required for the  installation  of
control equipment.  The additional land required for the disposal  of
solids collected from control devices will be  insignificant compared
with the land  required for the disposal of tailings from the
beneficiation  of metal!fc minerals.
7.6.2  Environmental Impact  of Delayed Standards
     The impacts on air pollution, water  pollution, solid waste  disposal,
and energy use associated with delaying proposal and promulgation  of
standards are  discussed in each of their  respective sections as  the
impacts of Regulatory Alternative 1.
                                  7-16

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7.7  REFERENCES FOR CHAPTER 7
Battelle  Columbus  Laboratories,   1975.   Energy  Use  Patterns  in
     Metallurgical and  Nonmetallic Mineral  Processing  (Phase  4 - Energy
     Data and  Flowsheets,  High Priority Commodities).  Report Compiled
     for  U.S.  Bureau of Mines, U.S.  Department of Commerce,  National
     Technical Information Service  PB-245 759.  179 p.

Battelle" Columbus  Laboratories,   1976.   Energy  Use  Patterns  in
     Metallurgical and  Nonmetallic Mineral  Processing  (Phase  6 - Energy
     Data and  Flowsheets,  Low Priority Commodities).  Report Compiled
     for  U.S.  Bureau of Mines.^U.S.  Department  of Commerce, National
     Technical Information Service  PB-261 150.  257 p.

Bowers, J.  F., J. R. Bjorklund,  and C.  S.  Cheney.  Industrial  Source
     Complex  (ISC)  Dispersion Model User's Guide.  U. S. Environmental
     Protection Agency, Research  Triangle Park, North  Carolina.   2 Vols.
     EPA-450/4-79-030 and EPA-450/4-79-031.   December, 1979.

Environmental  Protection Agency,  1980.  Development Document  for Proposed
     Effluent  Limitations Guidelines and New  Source Performance  Standards
     for  the Ore  Mining and Dressing Point  Source Category  (Draft Document),
     Washington,  D.C. 602 p.

Summerhays, J.   U.  S.  Environmental  Protection Agency.   1981.   Memo  to
     S. Cuffe,  U. S. Environmental  Protection Agency.   February 19.
     Dispersion Analyses for  Metallic Mineral  Processing  Plants.
                                  7-18

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                                8.   COSTS
8.1  COSTS OF AIR POLLUTION CONTROL FOR METALLIC MINERAL PROCESSING
     INDUSTRIES
8.1.1  Summary of Cost Results
     In this chapter, costs have been developed for the application of
each control option discussed in Chapter 6 to the emission points de-
scribed in the model plant parameters.  This section summarizes the
results of the cost analysis.   Methodology for development of the costs
for each control option will be discussed in Section 8.1.3.  All costs
presented in Section 8.1 are in fourth-quarter 1979 dollars.
     Tables 8-1 through 8-19 present capital and annualized costs that
have been developed for the regulatory alternatives for each new model
plant size.  As stated previously in Chapter 5, expansion of a metallic
mineral processing plant would involve the addition of a complete new
crushing line.  All control equipment costs in this case would be the
same as for a new source.  Because of the National Ambient Air Quality
Standard for lead, lead ore processing plants may be required to apply
more effective (and presumably, more expensive) control systems than
would be required by the State Implementation Plans (SIP's) for attaining
the NAAQS for generic particulate matter.  This higher level  of control
would be required even in the absence of an NSPS for metallic mineral
plants.  Thus, the actual incremental costs (that is the cost above
baseline control) incurred by lead ore processing plants in meeting the
emission level corresponding to a Regulatory Alternative 2 or 3 could be
less than those presented in this chapter.
     The costs presented in Tables 8-1 through 8-19 do not include the
costs of an initial compliance test.  As indicated in Appendix D, the
cost of a test of particulate emission concentration (replicated three

-------
times) would range from $5,000 to $9,000.   A survey of the current State
Implementation Plan regulations indicates  that most states would require
a compliance test for a new plant.  Therefore this cost would be similar
for all three regulatory alternatives.
     Credit for recovered product also has been included in Tables 8-1
through 8-19, and net annualized costs, representing the annualized
costs minus any credit for recovered product, are shown.  The net
annualized cost of a regulatory alternative describes the overall cost
of controlling an entire metallic mineral  processing plant with a given
control option.  As indicated in Tables 8-1 through 8-19 the highest net
annualized cost is that of control option 3b which is based on
the cost of 30-inch pressure drop wet scrubber.  This cost is a worst
case estimate because it is likely that a plant would have the option of
installing other types of control equipment to meet the emission levels
of Regulatory Alternative 3.  For example, baghouses could be used, in
preference to high energy wet scrubbers in process streams with low
moisture.  In exhaust streams characterized by low inlet concentrations
and/or large particle sizes, low energy wet scrubbers could be used in
preference to high energy wet scrubbers.  In general, the total industry
cost of meeting the emission level represented by a regulatory alternative
is not the cost of the control option upon which the alternative is
based multiplied by the number of new plants because many new plants may
be able to use less expensive control devices to meet that emission
level.
     Tables 8-20 through 8-29 present the marginal cost effectiveness (CE)
of each regulatory alternative, determined by the following equation:

                               CE =  -
where A equals the cost of the regulatory alternative of interest, B
equals the cost of Regulatory Alternative 1 (baseline), X equals emissions
expected with Regulatory Alternative 1, and Y equals the emissions
expected with the regulatory alternative of interest.
8.1.2  Product Recovery Credits and Dust Disposal Costs
     Product recovery credits have been attributed to only two emission
sources -  dryers and product loadout - because concentrated product is

                                 8-2

-------
handled only at these points.  Table 8-30 presents the data used in
developing product recovery credits.  Tables 8-1 through 8-19 show that
the product recovery credits are relatively insignificant to the total
control costs.  For those sources where no product recovery is assigned,
the credits achieved from the recycle of collected material are offset
by the cost of recycling this material.
8.1.3  Costs of Control Options:  Scrubbers and Baghouses
     Capital and annualized costs have been developed for the control of
each process emission source (including crushers, dryers, ore bins, and
product loadout) using each of the  four control options.  The control
options are:  (1) a centrifugal fan (mechanically aided) wet scrubber
(baseline), (2) a 3.75-kPa (15-inch) pressure drop venturi scrubber,
(3a) a 1.5-kPa (6-inch) pressure drop baghouse, and  (3b) a 7.50-kPa
(30-inch) pressure drop venturi scrubber.  Specifications for these
control options are shown in Table  8-31.  The selection of one of the
above control options to attain a given emission level will depend on
the inlet loading and particle size distribution.  The performance of
the control options will vary over the range of circumstances within the
metallic mineral industry.  Therefore, the selection of low energy
scrubbers can be used where conditions permit.  For  a discussion of
model plants and control options, see Chapter 6.
     Equipment costs were obtained  from vendors of pollution control
.equipment (Valerioti, 1979) and from published sources (Neveril, 1978).
Equipment costs for the venturi scrubbers were obtained from Neveril
(1978) and  include the cost of the  basic scrubber (venturi elbow,
separator,  and controls), a fan, a  pump, and the associated motors
required to operate the system.  The cost of the venturi scrubbers are
based on volumetric flow rate, operating pressure, and materials of
construction.  The costs presented  assume the material of construction
is carbon steel; however, when venturi scrubbers are used on dryers of
sulfur-containing concentrates, corrosion can be a problem necessitating
a stainless steel fan and scrubber  unit.  These costs do not reflect the
use of stainless steel on the dryer unit.  Calculations show that the
net annualized cost to the entire plant would increase by about three
percent by  using a stainless steel  fan and scrubber  on the dryer.
                                  8-3

-------
       The cost of the basic unit for a centrifugal  fan wet scrubber
  including an integral  fan was supplied by ^alerioti  (1979).   The  cost  of
  a fan motor and the cost of pumps  and associated motors  were  estimated
  from Meveril  (1978) and were added to the base  cost  of the centrifugal
  fan  wet scrubber to obtain the total  equipment  cost.   Equipment costs
  for  the baghouse were  provided by  Neveril  (1978) and include  the  basic
  baghouse structure,  insulation,  the bags,  a  fan, and motor to provide
  air  flow through the system.   Bag  cleaning:by pulse  jet  is  accomplished
  by the  use  of compressed  air jets  located  at the top  of  the bags.  No
  costs have  been  assigned  for an  air compressor  because it  is  assumed
  compressed  air is available  in the  plant.
      Component capital costs, shown in Tables 8-32 through 8-35, have
  been developed from published information  (Weaver,  1973;  Peters, 1968).
 These factors account for material  costs and labor expenses other than
 the basic equipment purchase cost.   Items t;hat are typically associated
 with a project, such as instrumentation, etectrical work, and site
 preparation are included as well as engineering expenses  and contractor's
 fees.  Application of these factors to the Equipment costs provided the
 capital  investment (including direct and indirect capital costs) for
 each  control system.  Annualized costs alsof have been developed  for
 these control  systems based upon the parameters  shown in  Table 8-36.
 8.1.4  Capital  Costs for Metallic Mineral  Processing  Plants
      Table 8-37 presents metallic mineral  processing  plant costs  derived
 from  Bureau of Mines contacts and literature  sources.   These plant
 capital  costs  have been obtained for the ten  metallic mineral  industries
 showing  growth  rates and include  both  mine  &nd mills  costs  in  all  cases
 except for the aluminum industry  as  explained in Section  8.1.4.1.
      The  capital  costs  presented  in  Table 8i37 were developed  by plotting
 separately the plant size  versus  capital investment for each metal and
 then  curve fitting the  data points.   In a few cases the reference  sources
 providing  capital cost  data did not  correlate very well.  In such cases,
more than  one curve was plotted for  each particular reference  source.
Thus,  there are low, average, and high capital cost estimates  for copper
and molybdenum in Table 8-37.
                                 8-4

-------
     A selected bibliography for Table 8-37 is provided at the end of
this chapter.   An entire set of references plus the calculations that
form the basis for the estimates are provided in the docket.
     8.1.4.1  Mine Capital Costs.  Mine capital costs include acquisition
of the property, exploration and development, equipment and construction
costs, facilities and utilities, and working capital.  Acquisition costs
are a nominal  fee to acquire lease rights.  Exploration costs are based
on an estimate of the work required to provide sufficient data to show
that the quantity and quality of the resources will economically justify
a mining operation for a particular deposit.  The major part of the
exploration cost consists of drilling and engineering expenditures.
There are no mine capital costs included for aluminum processing plants
because 90 percent of bauxite used in this country is imported.
     An estimate of the development cost includes the work necessary to
prepare the deposit for production.  For example, in the case of an
open-pit mine this work consists primarily of removing overburden (waste
material) to expose the ore body; however, for an underground operation
it includes the costs of shaft sinking and of driving drifts and raises.
Both types of mines are equipped with hoisting facilities, as well as
hauling, pumping, and ventilating equipment.  Equipment and construction
costs include the cost of all mobile equipment in the pit and the cost
of permanent structures.  Working capital is a function of operating
cost and therefore does not vary directly with the capital investment.
     8.1.4.2  Mill Capital Cost.  Mill capital costs include the cost of
all crushing,  grinding, flotation, and leaching facilities and equipment.
Aluminum capital costs are based on the Bayer process which is the
predominant process used in the United States to produce alumina from
bauxite (Kurtz, 1980).  In general, capital costs for all other metals
are the costs of constructing and installing all operations and equipment
required to produce the final products listed in Table 3-3.  Working
capital also is part of the total mill cost; however, it is a function
of operating cost and not a function of capital investment.
     Table 8-38 shows the total capital requirements itemized for a
25 ton/hr tungsten plant.
                                 8-5

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-------
        Table 8-20.   MARGINAL COST EFFECTIVENESS  OF REGULATORY ALTERNATIVES
        FOR THE ALUMINUM  ORE PROCESSING  INDUSTRY  MODEL  PLANTS  (1979 DOLLARS)
Regulatory
alternative
ruimber
Baseline
la

lba

2






3a






3b .






Quantity

Total parti cul ate emissions allowed under SIP's:
Mg/yr (ton/yr)
Total participate emissions from 6" wet scrubber:
Mg/yr (ton/yr)
Total particulate emissions: Mg/yr (ton/yr}
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Total particulate emissons: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Total particulate emissions: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Model plant
140 Mg/hr
(150 ton/hr) '

. 587 (645)

153 (168)

60 (67)
93 (101)
60
17

0.18 (0.08)

20 (22)
133 (146)
87
21

0.16 (0.07)

20 (22)
133 (146)
87
53

0.40 (0.18)

size
270 Mg/hr
(300 ton/hr)

667 (733)

263 (289)

105 (116)
158 (173)
60
31.

0.20 (0.09)

36 (39)
227 (250)
87
68

0.30 (0.14)

36 (39)
227 (250)
87
95

0.42 (0.19)

aEmission reduction and cost effectiveness are based on this baseline control level.
 Note:  All marginal cost effectiveness (CE) numbers are calculated using the equation in Section 8.1.1.
                                             8-25

-------
       Table  8-21.  MARGINAL  COST EFFECTIVENESS OF REGULATORY  ALTERNATIVES
       FOR THE COPPER  ORE PROCESSING  INDUSTRY  MODEL  PLANTS  (1979 DOLLARS)
Regulatory
alternative
number
Baseline
la

lba

2






3a






3b






Quantity

Total particulate emissions allowed under SIP's:
Mg/yr (ton/yr)
Total particulate emissions from 6" wet scrubber:
Mg/yr (ton/yr)
Total particulate emissions: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Total particulate emissons: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Total particulate emissions: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Model
140 Mg/hr
(150 ton/hr)

1,284 (1,413)

519 (570)

205 (225)
314 (345)
60
58

0.18 (0.08)

68 (75)
451 (495)
87
105

0.23 (0.11)

68 (75)
451 (495)
87
,167

0.37 (0.17)

plant size
540 Mg/hr
(600 ton/hr)

2,457 (2,703)

1,021 (1,124)

408 (449)
613 (675)
60
103

0.17 (0.08)

136 (150)
885 (974)
87
199

0.22 (0.10)

136 (150)
885 (974)
87
303

0.34 (0.16)

Emission reduction and cost effectiveness  are based on this baseline control level.   ....   fl -  ,
 KoteT All marginal cost effectiveness (CE) numbers are calculated using the equation in Section 8.1.1.
                                               8-26

-------
       Table 8-22.   MARGINAL COST EFFECTIVENESS  OF REGULATORY  ALTERNATIVES
          FOR THE GOLD ORE PROCESSING  INDUSTRY  MODEL PLANTS  (1979 DOLLARS)
Regulatory
alternative
number
Baseline
la

lba

2






3a






3b






Quantity

Total particulate emissions allowed under SIP's:
Mg/yr (ton/yr)
Total particulate emissions from 6" wet scrubber:
Mg/yr (ton/yr)
Total particulate emissions: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Total particulate emissons: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Total particulate emissions: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Model
68 Mg/hr
(75 ton/hr)

510 (561)

195 (215)

78 (86)
117 (129)
60
25

0.21 (0.10)

26 (29)
169 (186)
87
57

0.34(0.15)

26 (29)
169 (186)
87
66

0.39 (0.18)

plant size
140 Mg/hr
(150 ton/hr)

584 (642)

236 (260)

95 (104)
141 (156)
60
33

0.23 (0.11)

32 (35)
204 (225)
87
71

0.35 (0.16)

32 (35)
204 (225)
87
82

0.40 (0.18)

Emission reduction and cost effectiveness are based on this baseline control level.

 Note:  All marginal cost effectiveness (CE) numbers are calculated using the equation in Section 8.1.1.
                                              8-27

-------
       Table 8-23.   MARGINAL COST  EFFECTIVENESS OF  REGULATORY ALTERNATIVES
         FOR THE IRON ORE  PROCESSING INDUSTRY MODEL PLANTS  (1979 DOLLARS)
Regulatory
alternative
number
Baseline
la
iha
Quantity

Total particulate emissions allowed under SIP's:
Mg/yr (ton/yr)
Total oarticulate emissions' from 6" wet scrubber:
Model plant size
1,100 Mg/hr 2,200 Mg/hr
(1,200 ton/hr) (2,400 ton/hr)

1,859 (2,045) 3,324 (3,657)
1,313 (1,444) 2,666 (2,932)
   3a
   3b
  Mg/yr (ton/yr)
Total particulate emissions:  Mg/yr (ton/yr)
Emission reduction from baseline:   Mg/yr  (ton/yr)
Emission reduction from baseline:   (%)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg ($/lb) of particulate removed
Total particulate emissons:  Mg/yr (ton/yr)
Emission reduction from baseline:   Hg/yr  (ton/yr)
Emission reduction from baseline:   (%)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg ($/lb) of particulate removed
Total'particulate emissions:  Mg/yr (ton/yr)
Emission reduction from baseline:   Mg/yr (ton/yr)
Emission reduction from baseline:   (&)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg ($/lb) of particulate removed
  525  (578)
  788  (866)
    60
    136

 0.17  (0.08)

  175  (193)
1,138  (1,251)
    87
    290

 0.25  (0.12)

  175  (193)
1,138  (1,251)
     87
    441

 0.39  (0.18)
1,066 (1,173)
1,600 (1,759)
     60
    353

 0.22 (0.10)

  355 (391)
2,311 (2,541)
     87
    636

 0.28 (0.13)

  355 (391)
2,311 (2,541)
     87
    945

 0.41 (0.19)
Emission reduction and cost effectiveness are  based on this baseline control level.
 SteT  All  marginal cost effectiveness (CE)  numbers are calculated using the equation in Section  8.1.1.
                                                 8-28

-------
     Table 8-24.   MARGINAL COST EFFECTIVENESS  OF  REGULATORY ALTERNATIVES
    FOR THE LEAD/ZINC  ORE  PROCESSING  INDUSTRY  MODEL PLANTS  (1979 DOLLARS)

Regul atory
alternative
number
Basel 1 ne
la

lba



Total particulate
Mg/yr (ton/yr)
Total parti cul ate

Quantity

emissions allowed under SlP's:

emissions from 6" wet scrubber:

270
(300

1,254

470
Model plant
Mg/hr
tons/hr)

(1,380)

(517)
size
540
(600

1,682

698

Mg/hr
tons/hr)

(1,850)

(767)
   3a
   3b
  Mg/yr (ton/yr)
Total  particulate emissions:  Mg/yr (ton/yr)
Emission reduction from baseline:   Mg/yr  (ton/yr)
Emission reduction from baseline:   (%)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg ($/lb)  of particulate removed
Total particulate emissons:  Mg/yr (ton/yr)
Emission reduction from baseline:   Mg/yr  (ton/yr)
Emission reduction from baseline:   (%)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg ($/lb)  of particulate removed
Total particulate emissions:  Mg/yr (ton/yr)
Emission reduction from baseline:   Mg/yr  (ton/yr)
Emission reduction from baseline:   (%)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg ($/lb).of  particulate removed
 188 (207)
 282 (310)
    60
   65

0.23 (0.11)

  63 (69)
 407 (448)
    87
   142

0.35 (0.16)

  63 (69)
 407 (448)
    87
   174

0.43 (0.19)
 279 (307)
 419 (460)
    60
   102

0.24 (0.11)

 93 (102)
 605 (665)
    87
   225

0.37 (0.17)

 93 (102)
 605 (665)
    87
   264

0.44 (0.20)
Emission  reduction and cost effectiveness are based on this  baseline control level.
 Note:   All marginal cost effectiveness  (CE) numbers are calculated using the equation  in Section 8.1.1.
                                                   8-29

-------
      Table 8-25.  MARGINAL COST EFFECTIVENESS  OF REGULATORY ALTERNATIVES
     FOR THE MOLYBDENUM ORE PROCESSING  INDUSTRY MODEL  PLANTS (1979 DOLLARS)
Regulatory
alternative
number
Baseline
la

lba

2






3a






3b


,



Quantity

Total particulate emissions allowed under SIP's:
Mg/yr (ton/yr)
Total particulate emissions from 6" wet scrubber:
Mg/yr (ton/yr)
Total particulate emissions: Mg/yr" (tolf/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Total particulate emissons: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Total particulate emissions: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (20
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Model plant
270 Mg/hr
(300 ton/hr)

1,263 (1,390)

687 (756)

275 (302)
412 (454)
60
79

0.19 (0.09)

92 (101)
595 (655)
87
128

0.08 (0.04)

92 (101)
595 (655)
87
218

0.37 (0.17)

size
1,100 Mg/hr
(1,200 ton/hr)

2,165 (2,380)

1,400 (1,540)

560 (615)
840 (925)
60
147

0.17 (0.08)

187 (205)
1,213 (1,335)
87
311

0.26 (0.12)

187 (205) •
1,213 (1,335)
87
464

0.38 (0.17)

Emission reduction and cost effectiveness are based on this baseline control level.   .  .  . .   0 ,  ,
 Note:  All marginal cost effectiveness (CE) numbers are calculated using the equation in Section 8.1.1.
                                            8-30

-------
        Table  8-26.   MARGINAL  COST EFFECTIVENESS  OF  REGULATORY ALTERNATIVES
              THE  SILVER ORE PROCESSING INDUSTRY MODEL PLANTS  (1979 DOLLARS)
Regulatory
alternative
  number
                     Quantity
                                                                            Model plant size
 45 Mg/hr
(50 ton/hr)
 140 Mg/hr
(150 ton/hr)
Baseline

   la
   Ib
     a
   3a
   3b
Total particulate emissions allowed under SIP's:          472 (519)          586 (645)
  Mg/yr (ton/yr)

Total particulate emissions from 6" wet scrubber:         194 (213)          305 (336)
  Mg/yr (ton/yr)

Total particulate emissions:  Mg/yr (ton/yr)               77 (85)           122 (134)
Emission reduction from baseline:  Mg/yr (ton/yr)       •  117 (128)          183 (202)
Emission reduction from baseline:  (%)                      60                60
Costs of regulatory alternative above baseline               26                34
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:            0.22 (0.10)        0.19 (0.08)
  $/kg ($/lb)  of particulate removed
Total particulate emissons:  Mg/yr (ton/yr)                25 (28)            41 (45)
Emission reduction from baseline:  Mg/yr (ton/yr)         169 (185)          264 (291)
Emission reduction from baseline:  (%)                      86                86
Costs of regulatory alternative above baseline               59                95
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:            0.35 (0.16)        0.36 (0.16)
  $/kg ($/lb)  of particulate removed
Total particulate emissions:  Mg/yr (ton/yr)               25 (28)            41 (45)
Emission reduction from baseline:  Mg/yr (ton/yr)         169 (185)          264 (291)
Emission reduction from baseline:  (%)                      86                86
Costs of regulatory alternative above baseline               76                108
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:            0.45 (0.20)        0.41 (0.19)
  $/kg ($/lb)  of particulate removed
aEmission reduction and cost effectiveness are based on this baseline control  level.
 Note:   All  marginal cost effectiveness (CE) numbers are calculated using the  equation in Section 8.1.1.
                                                   8-31

-------
       Table 8-27.  MARGINAL COST EFFECTIVENESS  OF REGULATORY ALTERNATIVES
FOR THE TITANIUM/ZIRCONIUM ORE PROCESSING INDUSTRY MODEL PLANTS  (1979 DOLLARS)
Regulatory
alternative
number
Baseline
la

lba

2






3a






3b






Quantity

Total particulate emissions allowed under SIP's:
Mg/yr (ton/yr)
Total particulate emissions from 6" wet scrubber:
Mg/yr (ton/yr)
Total particulate emissions: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Total particulate emissons: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Total particulate emissions: Mg/yr (ton/yr)
Emission reduction from baseline: Mg/yr (ton/yr)
Emission reduction from baseline: (%)
Costs of regulatory alternative above baseline
cost: (thousand $/yr)
Cost effectiveness of regulatory alternative:
$/kg ($/lb) of particulate removed
Model
270 Mg/hr
(300 ton/hr)

427 (470)

280 (308)

112 (123)
168 (185)
60
43

0.25 (0.11)

37 (41)
243 (267)
87
71'

0.29 (0.13)

37 (41)
243 (267)
87
102

0.42 (0.19)

plant size
540 Mg/hr
(600 ton/hr)

601 (661)

449 (493)

179 (197)
270 (296)
60
39

0.14 (0.07)

60 (66)
389 (427)
87
103

0.27 (0.12)

60 (66)
389 (427)
87
156

0.40 (0.18)

   Emission reduction and cost effectiveness are based on this baseline control level.
    Note:  All marginal cost effectiveness  (CE) numbers are calculated using the equation in Section 8.1.1.
                                                8-32

-------
         Table 8-28.   MARGINAL  COST EFFECTIVENESS OF REGULATORY  ALTERNATIVES
         FOR THE TUNGSTEN ORE PROCESSING INDUSTRY MODEL  PLANTS  (1979 DOLLARS)
Regulatory
alternative
  number
                    Quantity
 Model  plant  size
23 Mg/hr (25  ton/hr)
Baseline
   la

   lba

   2
   3a
   3b
Total particulate emissions allowed under SIP's:
  Mg/yr (ton/yr)
Total particulate emissions from 6" wet scrubber:
  Mg/yr (ton/yr)
Total particulate emissions:  Mg/yr (ton/yr)
Emission reduction from baseline:  Mg/yr (ton/yr)
Emission reduction from baseline:  (%)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg ($/lb)  of particulate removed
Total particulate emissons:  Mg/yr (ton/yr)
Emission reduction from baseline:  Mg/yr (ton/yr)
Emission reduction from baseline:  (%)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg ($/lb)  of particulate removed
Total particulate emissions:  Mg/yr (ton/yr)
Emission reduction from baseline:  Mg/yr ('ton/yr)
Emission reduction from baseline:  (%)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg ($/lb)  of particulate removed
    562 (618)

    163 (180)

     65 (72)
     98 (108)
        60
         7

    0.07 (0.03)

     22 (24)
    141 (156)
        87
        24

    0.17 (0.08)

     22 (24)
    141 (156)
        87
        41

    0.29 (0.13)
aEmission reduction and  cost effectiveness are based  on this baseline control  level.
 Note:  All marginal  cost effectiveness (CE) numbers  are calculated using the  equation  in Section 8.1.1.
                                                 8-33

-------
        Table  8-29.   MARGINAL  COST EFFECTIVENESS  OF  REGULATORY ALTERNATIVES
        FOR THE URANIUM ORE PROCESSING INDUSTRY MODEL PLANTS  (1979 DOLLARS)
Regulatory
alternative
  number
                     Quantity
                                                                            Model plant size
   23 Mg/hr
  (25 ton/hr)
                                                                            68 Mg/hr
                                                                           (75 ton/hr)
Baseline
   la

   lba

   2
   3a
   3b
Total particulate  emissions allowed under SIP'.s:
  Mg/yr (ton/yr)
Total particulate  emissions from 6" wet scrubber:
  Mg/yr (ton/yr)
Total particulate  emissions:  Mg/yr (ton/yr)
Emission reduction from baseline:  Mg/yr (ton/yr)
Emission reduction from baseline:  (%)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg ($/lb) of particulate removed
Total particulate  emissons:  Mg/yr (ton/yr)
Emission reduction from baseline:  Mg/yr (ton/yr)
Emission reduction from baseline:  (%)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg ($/lb) of particulate removed
Total particulate  emissions:  Mg/yr (ton/yr)
Emission reduction from baseline:  Mg/yr (ton/yr)
Emission reduction from baseline:  (%)
Costs of regulatory alternative above baseline
  cost:  (thousand $/yr)
Cost effectiveness of regulatory alternative:
  $/kg (5/lb) of  particulate removed
 140 (154)

 78 (86)

  31 (34)
  47 (52)
    60
    11

0.23 (0.10)

  10 (11)
  68 (75)
    87
   17

0. 25 (0.11)

  10 (11)
  68 (75)
    87
   28

0.41 (0.19)
 183  (201)

 120  (132)

  48  (53)
  72  (79)
   60
   14

0.19  (0.09)

  16  (18)
 104  (114)
   87
   33

0.31  (0.14)

  16  (18)
 104 (114)
    87
    36

0.35  (0.16)
Emission reduction and cost effectiveness are based on this baseline control level.    _
 Note:  All marginal cost effectiveness  (CE) numbers are calculated  using the equation in Section  8.1.1.
                                                   8-34

-------
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        Table  8-32.   DIRECT CAPITAL COST FACTORS FOR A WET SCRUBBER
                    AS A FUNCTION  OF EQUIPMENT COST (Q)a'°
Component
Equipment
Ductwork
Instrumentation
Electrical
Foundations
Structural
Sitework
Painting
Piping
Total direct costs
Material
1.00 Q
0.10 Q
0.05 Q
0.06 Q
0.03 Q
0.06 Q
0.02 Q
0.005 Q
0.09 Q
1.42 Q
Labor
0.09 Q
0.09 Q
0.02 Q
0.12 Q
0.05 Q
0.03 Q
0.02 Q
0.02 Q
0.08 Q
0.52 Q
   Weaver, 1973.
  3Peters and Timmerhaus, 1968.

       Table 8-33.   INDIRECT CAPITAL COST FACTORS FOR A WET SCRUBBER
                    AS A FUNCTION OF EQUIPMENT COST (Q)a>
Component
   Measure of costs
                                                                  Factor
Engineering
Contractor's fee
Shakedown
Spares
Freight
Taxes
Total indirect costs
Contingencies
Total capital costs
10% of material and labor
15% of material and labor
5% of material and labor
1% of material
3% of material
3% of material
0.19 Q
0.29 Q
0.10 Q
0.01 Q
0.04 Q
0.04 Q
0.67 Q
0.52 Q
3.13 Q
aWeaver, 1973.
 Peters, and Timmerhaus, 1968.
C20% of direct and indirect costs.
                                     8-37

-------
       Table 8-34.   DIRECT CAPITAL COST FACTORS FOR A BAGHOUSE AS  A
                      FUNCTION OF EQUIPMENT COST (Q)a>D
Component
Equipment
Ductwork
Instrumentation
Electrical
Foundations
Structural
Sitework
Painting
Total direct costs
Material
1.00 Q
0.14 Q
0.05 Q
0.05 Q
0.03 Q
0.06 Q
0.02 Q
0.005 Q
1.36 Q
Labor
0.'09 Q
0.11 Q
0.02 Q
0.10 Q
0.05 Q
0.03 Q
0.02 Q
0.02 Q
0.44 Q
  leaver, 1973.
   Peters and Timmerhaus, 1968.
      Table 8-35.  INDIRECT CAPITAL COST FACTORS FORA.BAGHOUSE AS A
                      FUNCTION OF EQUIPMENT COST (Q)a'D
Component
   Measure of costs
                                                                  Factor
Engineering
Contractor's fee
Shakedov/n
Spares
Freight
Taxes
Total indirect costs
Contingencies0
Total capital costs
10% of material and labor
15% of material and labor
5% of material and labor
1% of material
3% of material
3% of material
0.18 Q
0.27 Q
0.09 Q
0.01 Q
0.04 Q
0.04 Q
0.63 Q
0.49 Q
2.92 Q
aWeaver, 1973.
 Peters and Timmerhaus, 1968.
°20% of direct and indirect costs.
                                    8-38

-------
     Table 8-36.   BASES FOR SCRUBBER AND FABRIC FILTER ANNUALIZED COSTS
                               (1979 dollars)
Type of cost
                 Description
Direct operating cost

  Utilities

    Water
    Electricity
  Operation and maintenance

    Scrubber

    Fabric filter
Water from the tailings pond is typically
used for scrubbers as well as for the ore
processing equipment.  No cost is assigned
to the (small) fraction used for scrubbers.

$0.0302/kWh (Scrubber electricity usage is
derived from pump and fan requirements and
annual hours of operation.  Fabric filter
electricity usage is derived from fan and
compressor requirements and annual hours
of operation.)
14.85% of capital investment

15.75% of capital investment
Capital charges

  Capital recovery factor

  Taxes, Insurance, and
  Administration
16.69% of capital investment

4% of capital investment
 Based on a 15-year lifetime for either scrubbers or fabric filters, and
 an interest rate of 14.5 percent.
                                      8-39

-------
  Table 8-37.   FIXED CAPITAL INVESTMENT*
(Using fourth-quarter 1979 dollars x 106)
Mi neral
Aluminum




Copper
low
average
high
low
average
high
low
average
high
low
average
high
Gold





Plant
size (ton/hr)

50
150
300
600

150
150
150
300
300
300
600
600
600
1,200
1,200
1,200

10
50
75
150
300
Mine






32
44
46
40
55
59
47
52
78
69
109
119






Mill

145
430
870
1,750

15
21
23
22
33
35
40
,61
66 '
72
114
124






Combined






47
65
69
60
88
94
87
133
144
141
223
243

10
27
34
52
79
                (continued)
                    8-40

-------
Table 8-37.  Continued

Mineral
Iron



Lead/Zinc



Molybdenum
low
average
high
low
average
high
low
average
high
low
average
high
Plant
size (ton/hr) Mine

600
1,200
2,400

150 19
300 50
600 114

150
150
150
300
300 I
300
600
600
600
1,200
1,200
1,200
Mill Combined

345
707
1,430

16 35
45 95
100 214

36
68
130
72
100
140
90
125
144
245
285
426
      (continued)
           8-41

-------
                       Table 8-37.   Concluded
Plant
Mineral size (ton/hr) Mine
Silver



Ti tani um/Zi rconi urn

Tungsten
Uranium

35
50
150
200
300
600
25
25
75
Mill Combined
17
25
76
102
10
• 17
15
6.8
20
References for this table are found in a bibliography at the end of
 this section.
                                8-42

-------
  Table 8-38.   TOTAL CAPITAL REQUIREMENTS FOR A 25 TPH TUNGSTEN PLANT"
Unit
Cost (1979 4th quarter
    (dollars x 106)
Mine
  Surface mine plant and buildings
  Underground equipment and construction
  Mine property acquisition
  Mine exploration and development

     Total
             0.5
             0.3
             0.1
             0.9

             1.8
Mill
  Crushing section
  Grinding section
  Flotation section
  Leaching section

     Total
             0.4
             0.3
             0.3
             0.1

             1.1
Plant facilities
Plant utilities
     Total
             0.3
             0.4
             0.7
Total plant cost (insurance and tax bases)
Interest during construction
Working capital
     Total
             3.6
             0.2
             0.6

             4.4
 Stefford, 1971.
                                 8-43

-------
8.2  OTHER COST CONSIDERATIONS
     The cost considerations assessed in this section for the 16 metallic
mineral industries are a result of pollution control  standards other
than this New Source Performance Standard (NSPS).   The other air pollu-
tion control costs considered include NSPS for primary copper, lead, and
zinc smelting industries, and iron and steel plants.   In addition, the
control costs resulting from the National Ambient Air Quality Standard
(NAAQS) for Lead will be considered.  The control  costs required by the
Occupational Safety and Health Administration (OSHA) standards and water
pollution control requirements are addressed.  The solids wastes
(tailings) resulting from the beneficiation of metallic minerals have
been exempted from the provisions of the Resource Conservation and
Recovery Act.
8.2.1  Other Air Pollution Control Costs
     8.2.1.1  NSPS.
     8.2.1.1.1  Primary copper smelters.  Total capital and operating
costs are presented in Table 8-39 for various combinations of emission
control processes for the four basic copper smelter type configurations -
electric smelting, flash smelting, roaster/reverberatory smelting, and
reverberatory smelting.  In addition, the overall control of  sulfur
dioxide emissions, expressed as a percent, achieved with each control
alternative is summarized.  Table 8-39 also presents control  costs and
incremental control costs expressed in terms of cents per pound of
copper produced and cents per pound of sulfur dioxide controlled.*  The
baseline control is by single stage acid plant and neutralization.
     8.2.1.1.2  Primary zinc smelters.  The cost of controlling sulfur
dioxide and particulate emissions at a new  source zinc  smelter depends
on both the particular smelting refining process that is utilized  in  the
new  source  smelter and the control  level chosen for the process.   Total
capital and operating costs are presented in. Table 8-40 for various
combinations of emission control processes  for the three basic zinc
smelter type configurations - electrolytic  process (roasting  and
leaching),  conventional roasting and sintering, and the Robson process
 ^Incremental  cost  throughout this  section  is  the difference  between the
 alternative  control  cost  and the appropriate  baseline  control cost as
 indicated  in the text.
                                 8-44

-------
(combined roast/sinter).  Table 8-40 also presents control costs and
incremental control costs expressed in terms of cents per pound of zinc
produced and cents per pound of sulfur dioxide controlled.  The baseline
control is by single stage acid plant and neutralization.
     8.2.1.1.3  Primary lead smelters.  The cost of controlling sulfur
dioxide and particulate emissions at a new source lead smelter depends
on both the smelting process that is used as well as the control level
chosen for the process.  Three smelting techniques were considered for
use in a new source lead smelter.  These techniques are recirculating
sintering machine, nonrecirculating sintering machine, and electric
furnace and converters.  The five control systems considered were single-
stage sulfuric acid plants, dual-stage sulfuric acid plants, elemental
sulfur plants coupled with dimethylamine (DMA) units, elemental sulfur
plants coupled with Wellman-Lord scrubbing units, and DMA units only.
Various combinations of emission control processes were coupled with the
three smelting techniques and are presented in Table 8-41.  Table 8-41
presents control costs and incremental control costs expressed in terms
of cents per pound of lead produced and cents per pound of sulfur dioxide
controlled.   The baseline control is by single stage acid plant and
neutralization.
     8.2.1.1.4  Primary aluminum industry.   The NSPS for primary aluminum
reduction plants limits emissions of total  fluorides and visible emissions
from potrooms that house primary aluminum reduction cells and from anode
bake plants.
     Primary aluminum reduction is carried out in shallow rectangular
cells (pots) made of carbon-lined steel  with carbon blocks that are
suspended above and extend down into the pot.   The pots and carbon
blocks serve as cathodes and anodes, respectively, for the electrolytical
process.   Three types of reduction cells or pots are used in the United
States:   prebake (PB), horizontal stud Soderberg (HSS), and vertical
stud Soderberg ~(VSS).   Table 8-42 shows  the capital  and annual  costs  for
control  of pre-bake cells,  and vertical  and horizontal stud Soderberg
cells.  The capital cost includes the primary collection system (hoods
and ducts),  the fans and other auxiliary equipment,  the collection
device,  and wastewater treatment facilities if required.   Because the
carbon anodes used in the prebake cells  are made in a separate operation,

                                8-45

-------
the anode baking furnace control equipment costs must be added to the
reduction cell emissions in order to determine the total cost for control
under this NSPS.  Table 8-43 presents the range of control costs for the
anode baking furnace.  Capital costs are given in terms of dollars/ton
of annual capacity of aluminum produced and annualized costs are given
in terms of 
-------
     8.2.1.1.7  Electric submerged arc furnaces for production of ferroalloys.
The NSPS for electric submerged arc furnaces limits emissions of particulate
matter from ferroalloy plants.  In ferroalloy production, the major
source of pollution is the electric submerged arc furnace which performs
the smelting operations.  There are three different furnace configurations -
open, semi-closed, and sealed.  The type of configuration present at the
ferroalloy plant affects the efficiency of air pollution control equipment.
Costs were developed for open and sealed furnaces for two types of
control devices - wet scrubbers and fabric filters.  Table 8-46 presents
costs for the variable throat venturi scrubber for an open and a sealed
furnace.  The maximum power rating for this furnace is 33 MW for HC FeMn
and 38 MW for SiMn.  The use of a fabric filter as a control device on a
sealed furnace has not been demonstrated in the United States.   The
estimated capital cost for a conventional fabric filter control  system,
consisting of a radiant cooler, cyclone, fan, fabric filter, dust and
collected storage equipment is estimated at about $250,000 (1974 dollars).
     8.2.1.2  Lead NAAQS.   An Economic Impact Assessment for the National
Ambient Air Quality Standard for Lead was completed on June 28,  1978
(Environmental Protection Agency, 1978).   The final promulgated standard
           3
is 1.5 ug/m  with an averaging period of 90 days.   The NAAQS for lead
could effect the level of emission control  required for primary lead
smelters and primary copper smelters as well as the lead ore processing
units covered in this document.  The control costs for meeting the lead
NAAQS for primary lead and primary copper smelters are given in Table 8-47.
The investment, annualized control cost,  and investment and annualized
cost as a percent of annual revenue for the model  lead smelter and the
model copper smelter are presented in Table 8-47.   The annual  production
rates for the model lead smelter and the model  copper smelter are 62,000
megagrams per year and 635,000 megagrams per year, respectively.   These
control costs are based on the best demonstrated control  system currently
available (building evacuation to a fabric filter).
8.2.2  Control Costs Resulting from OSHA Regulations
     OSHA undertook a formal  analysis of cost of compliance with the
        3
100 ug/m  permissible exposure limit (PEL)  to lead for the lead smelting
industry.   Since this analysis was done,  OSHA decided that the proposed
                                8-47

-------
level of 100 ug/m3 did not provide adequate worker protection and that a
50 ug/m3 PEL was required.  However, OSHA determined that the cost for
control to proposed 100 ug/m3 level adequately estimated the cost for
the lower standard for most industries.   In addition, OSHA found that
                                     o
compliance with levels below 100 ug/m  might require extensive tech-
nological development in several industries and long periods of implementation
time.  This time frame would preclude meaningful quantification of cost.
Therefore, the costs presented are for the 100 ug/m  concentration
level.
     To aid in its assessment of economic factors, OSHA contracted with
DB Associates Inc. (DBA) to investigate the technological feasibility of
compliance with the proposed PEL of 100 ug/m3 and to estimate compliance
costs for the lead smelting industry.  A draft of the Lead Industries
Association (LIA) study ("Economic Impact of Proposed OSHA Lead Standards")
conducted by Charles River Associates ("CRA") was also used for economic
data in the smelting industry.  Table 8-48 shows the cost estimates for
the primary lead sector made by DBA and CRA to meet the 100 ug/m  level.
     Estimating the cost impact of the lead OSHA standard for lead pro-
cessing plants is extremely difficult.  "Contacts with both the Bureau of
Mines and the Department of Labor reveal that little data relating to
the additional expenditures for this industry to comply with OSHA regula-
tions (43 Federal Register 52952) are available.  Furthermore, contacts
directly with the industry reveal a general lack of quantitative data.
Consequently, at this point a full assessment of the economic impact of
OSHA on this industry is  not possible.  In general, however, qualitative
information provided by these contacts indicates limited economic impact
due to OSHA, because additional expenditures over and above those normally
incurred by the lead processing plants are likely to be small.
8.2.3  Water Pollution Control  Requirements
     Generalized capital  and annual  costs for wastewater treatment
processes at ore mining and dressing facilities have been established.
Costing  has been prepared on a  unit  process basis for each  of the metallic
minerals.  The effluent limitations  that must be achieved by 1 July 1984
under  the Clean Water Act (CWA) require consideration of costs  in the
requirements for Best Available Treatment; however, the CWA does  not
require  a balancing of costs against effluent reduction  (see Weyerhauser

                                8-48

-------
vs.  Costle, 11 ERC 2149 (DC Cir.  1978)).  The regulations proposed for
July 1984 are, in fact, based on the application of what the Agency
deems to be Best Available Technology Economically Achievable.   New
Source Performance Standards (NSPS), required under Section 306 of the
CWA, are also based on the application of the Best Available Demonstrated
Control Technology.  EPA has proposed New Source Performance Standards
to be based on Best Available Demonstrated Control Technology for all
metallic mineral industries.
     A study of existing froth flotation mills in the copper, lead,
zinc, gold, silver, and molybdenum ore processing industries reveals
that a large percentage of these facilities are already effectively
achieving 100 percent recycle of mill water.  A number of the facilities
practicing 100 percent recycle are located in arid regions.
     Tables 8-49 to 8-55 summarize the treatment costs for specific
plant sizes for each of the metallic mineral processing industries.
These costs are for existing plants.  It is probable that the costs for
a new plant to meet the New Source Performance Standards (NSPS) are no
more than the costs for an existing plant.  In the construction of a new
plant, in-process modifications can often be made more efficiently and
economically than add-on treatment technologies for existing plants.
                                8-49

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           Table 8-42.   COST OF POTLINE CONTROLS FOR
                   ALUMINUM REDUCTION SMELTERS3
      Cell  type
                             Prebake
                                          Horizontal
                         Vertical             stud
                      stud Soderberg       Soderberg
Control equipment
1°-FBDS   1°-IADS   1°-FBDS   1°-ST+WESP   1°-ST+WESP
                    2°-SS      2-SS
Capital cost ($/ton)
   67-
 59
                                                         117
                                                                      193
Annual cost ($/ton)

  Operating and
    maintenance

  Depreciation    8%
  Administrative
    overhead      5%
  Property tax,
    insurance     2%
                  15%
  Interest

  Royalty
Gross annual'cost

  Credits (alumina
    @ $0.032/lb,
    and fluoride
    @ $0.25/lb
Net annual  cost
  ($/ton)
  5.57      4.35      9.70       11.69        11.89





 10.02      8.80     14.31   .    17.49        28.91



  5.36      4.70      7.64        9.32        15.46

   .33       --         .33
 10.74
  0.54
7.31
0.37
22.79
 1.14
                         21.28     17.85     31.98      38.50
(10.54)   (10.54)    ( 9.19)
38.50
 1.93
                                                                     56.'26
56.26
 2.81
 Singraaster,  D.  and  S.  Breyer, 1973.  All costs in 1972  dollars.

bEBOS - Fluidized Bed  Dry Scrubber
 IADS - Injected Alumina Dry Scrubber
 ST - Spray Tower
 WESP - Wet Electrostatic Precipitator
 SS - Spray Screen
 1° = primary control  system
 2° = secondary  control system
cln addition  a $100,000 one-time fee is charged per company  for this design.
                                            8-56

-------
            Table 8-43.  CONTROL COSTS FOF
            PREBAKE ANODE BAKING FURNACES'
           ,b
  Control Equipment
PC+DESP+WS or WS+WESP1
Capital cost ($/ton)

Annual cost (
-------
       Table 8-44.  CONTROL COSTS OF MEETING PERFORMANCE STANDARD
                (0.22 gr/dscf) FOR TYPICAL NEW TWO-VESSEL BASIC
                          OXYGEN PROCESS FURNACES3'b'C
Plant size,
tons/melt
140


250


Required
control
equipment
Open hood,
scrubber
Open hood,
ESP
Closed hood,
scrubber
Open hood,
scrubber
Open hood,
ESP
Closed hood,
scrubber
Control
investment,
$
4,700,000
5,900,000
6,800,000
7', 400, 000
8,000,000
8,400,000
Annual cost,
$/yr
1,950,000
1,500,000
2,140,000
2,750,000
2,000,000
2,800,000
Annual cost per
unit of
production,
$/ton
1. 52
1.17
1.67
1.20
0.89
1.22
aMajor assumptions:  (1) production of 140 tons/melt = 2,300,000 tons/yr;
 (2) 18-year straight-line depreciation.
 Environmental Protection Agency, 1973.
CA11 costs in 1973 dollars.
                                       8-58

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-------
         Table 8-46.   COMPARISON  OF  CAPITAL  AND  ANNUAL COSTS
                    FOR AN  OPEN AND SEALED  FURNACE*'u
                 Cost item
                                                   Open furnace
                                                                     Totally enclosed
                                                                          furnace
Comparison of total capital costs
(thousands of $)
Basic furnace and associated process equipment
Incremental furnace cost
Incremental feed pretreatment
Air pollution control systems

Comparison of control equipment costs
Capital costs (thousands of $)
Primary system
Taphole system (see Table VI-7)
Incremental furnace cost

Annual costs (thousands of $ per year)
Operating cost
Maintenance (6%)
Capital recovery (@ 8% interest)
Administration (2%)
Taxes and insurance (2%)

Annual cost per ton ($/ton)

HC FeMri
SiHn


$ 8,500

3,500
$12,000


$ 3,500
(inc. in above)

$ 3,500

$ 143
210,
409d
70
/u
$ 902

* Q T-l
$20.50


$ 8,500
1 400
3 000
2,100
$15,000


$ 1,700C
400
1 400

$ 3,500

$ 135
210
390e
70
70

$ 875

$ 8.84!
$19.89T
aEnvironmental  Protection Agency, 1974c.

bAll costs in 1974  dollars.   v.

Includes $900,000  for the cooler,, mechanical  separator, scrubber, mist eliminator  and
 water treatment equipment; $420,000 for the furnace cover and.mechanical  seals; and
 $380,000 for the prorated share of electrical  utility and engineering costs.

Depreciation life:   15 years.

Depreciation lives:  10 years - furnace cover, 15  years - pollution control  system,
 20 years - incremental furnace costs.

fThis does not include the annualized investment cost or operating cost of the incremental
 feed pretreatment equipment.  The ferroalloy ^<»"st7has indicated that the total
 manufacturing cost per ton of product is about equal for both the open furnace vntn
 control and the sealed furnace with control and feed preparation.
                                             8-60

-------
        Table 8-47.  CONTROL COSTS OF THE LEAD NAAQS FOR MODEL PRIMARY

                     LEAD AND PRIMARY COPPER SMELTERS9'D'c

Investment As a % of Annual ized cost
Plant 103$ annual revenue 103$
Primary 1600 5.2% 400
Lead
Primary 7600 5.2% 1600
Copper
As a % of
annual revenue
1.2%
1.1%
 Environmental Protection Agency, 1978.

h                       3
 Costs based on 1.5 ug/m  final standard with an averaging period of one

 calender quarter.


CA11 costs in 1978 dollars.
                                   8-61

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-------
                    SELECTED REFERENCES FOR TABLE 8-37
 A.    Aluminum
 Peters,  F.  A.  and J.  Johnson.   1974.   Revised and Updated Cost Estimates
      for Producing Alumina from Domestic Raw Materials.   United States
      Bureau of Mines  Information Circular 8648.   Washington,  D.C.   58 p.


 B.    Copper

 Bennett,  H.  J.  and L.  Moore.   1973.   An Economic Appraisal  of the  Supply
      of  Copper from Primary Domestic  Sources.   United States  Bureau of
      Mines  Information Circular,  8598.   Washington,  D.C.   65  p.

 Dayton,  S.  H.   1980.   This Month in Mining - New and Expanding Mines and
      Plants.   Engineering  and  Mining  Journal,  181(3):39-63.

 Dayton,  S.  H.   1980.   This Month in Mining - Benguet's Dizon  Copper
      Project Goes  on  Stream.   Engineering and Mining Journal,
      181(2):36-39.

 Dayton,  S.  H.   1975.   This Month  in Mining - Hecla Mining is  Coming into
      Production at Lake Shore.   Engineering and  Mining Journal,  176(11):37.


 C.    Gold

 Dayton,  S.  H.   1980.   This Month  in Mining - New and Expanding Mines and
      Plants.   Engineering  and  Mining  Journal,  181(3):55.

 Li, T. M.   1980.   This Month in Mining- U.S.  and International  Minerals
      News Brief.   Mining Engineering  32(1): 17.

 Ski 11 ings,  D.  N.   1980.  Atlas Begins Output at  Masbate Gold Mine.
      Skillings1 Mining Review, 69(2):5.

 Skill ings,  D.  N.   1980.  Freeport Minerals  Reports Record Earnings.
      Skillings1 Mining Review, 69(9):12.

 Skillings, D.  N.   1980.  IU International  to Develop Gold Mine.  Skillings1
      Mining  Review, 69(38):13.
D.
Iron
Peterson, 0., R. J. Michaelson, and H. J. Volta.  1970.  Evaluating the
     Economic Availability of Mesabi Range Taconite Iron Ore with
     Computerized Models.  United States Bureau of Mines Information
     Circular 8480.  Washington, D.C.  60 p.,

(continued)
                                    8-71

-------
D.   Iron (continued)

Dayton, S. H.  1978.  This Month in Mining - New and Expanding Mines and
     Plants.  Engineering and Mining Journal, 179(10):25-33.

Dayton, S. H.  1975.  This Month in Mining - New and Expanding Mines and
     Plants.  Engineering and Mining Journal, 176(10):36.


E.   Lead/Zinc

Cammarota, V. A., U.S. Bureau of Mines.  1980.  Telephone conversation
     with M. Buckwalter, TRW.  September 17.  Capital cost  information
     for zinc mine and mill.

Dayton, S. H.  1980.  This Month in Mining - West Fork Will be First New
     U.S. Lead/Zinc Mine Since 1974.  Engineering and Mining Journal,
     181(4):41.

Dayton, S. H.  1980.  This Month in Mining - St. Joe will Develop a New
     Mine and Mill at Virburnum, Missouri.  Engineering and Mining Journal,
     181(6):43.

Rathjen, J.   U.S. Bureau of Mines.  1980.  Telephone conversation with
     M. Buckwalter, TRW.  September 17.  Capital cost information for
     lead mine and mill.
F.   Molybdenum

Kummer, J., U.S. Bureau of Mines.  1980.  Telephone conversation with
     E. Monnig, TRW.  September 16.  Capital cost information for
     molybdenum mine and mill.

Li, T. M.  1980.  U.S. and International Mineral News Briefs - U.S.
     Borax and Chemical Corporation.  Mining Engineering 32(2):148.

Schickner, B.C.  1980.  U.S. and International Mineral News Briefs -
     Standard Oil Company (Indiana).  Mining Engineering 32(9):1322.


G.   Nickel

Sibley, S., U.S. Bureau of Mines.  1980.  Telephone conversation with
     M. Buckwalter, TRW.  September 17.  Capital cost information for
     nickel mine and mill.
                                    8-72

-------
H.   Silver

Drake, H. J. , U.S. Bureau of Mines.   1980.  Telphone  conversation with
     M. Alexander, TRW.  September 25.   Capital  cost  information for
     silver mine and mill.
Li, T. M.  1980.  Industry Newswatch  - Asarco's  West  Fork  Lead Mine
     Sets 1983 Startup Date.  Mining  Engineering 32(4):377.

Schickner, B. C.  1980.  U.S. and International  Mineral  News Briefs -
     Wallace Diamond Drilling Company.   Mining Engineering 32(9):1320.


I.   Titanium/Zirconium

Whittle, E., Humphreys Mining Co.  1980.  Telephone conversation with
     E. Monnig, TRW.  December 12.  Capital Cost Information for Titanium/
     Zirconium Mines and Mills.

J.   Tungsten

Stafford, P., U.S. Bureau of Mines.   1980.  Telephone conversation with
     M. Alexander, TRW.  September 25.   Capital  cost  information for
     tungsten mine and mill.

Larson, L.  P. et al.  1971.   Cost Analysis for Various Tungsten Mines and
     Mills.  United States Bureau of  Mines Information Circular 8500.
     Washington, D.C.   65 p.


K.   Uranium

Klemenic, J., Director Supply Analysis Division, U.S.  Department of
     Energy.   1979.   Uranium Production  Capability in the United States,
     p. 205-229.

Pittman, R.,  Department of Energy.  1980.  Telephone conversation with
     M. Alexander, TRW.  September 22.   Capital  cost information for
     uranium mine and mill.
                                    8-73

-------
8.3  REFERENCES FOR CHAPTER 8

Bennett, H. J. and L. Moore.  1973.  An Economic Appraisal of the Supply
     of Copper from Primary Domestic Sources.  United States Bureau of
     Mines Information Circular 8598.  Washington, D.C.  65 p.

Bureau of Mines.  1980.  Mineral Commodity Summaries.  200 p.

Butterman, W.C., Bureau of Mines, 1981.  Telephone conversation with
     E. Monnig, TRW.  January 8.  Price information for metallic mineral
     processing concentrates.

Cammarota, V.A., Bureau of Mines.  1981.  Telephone conversation with
     M. Buckwalter, TRW.   January 7.  Price information for metallic
     mineral processing concentrates.
Dayton, S. H.  1979.  Engineering and Mining Journal Markets.
     and Mining Journal, 180:(5)19-25.
Engineering
Environmental Protection Agency.  1973.  Background Information for
     Proposed New Source Performance Standards:  Asphalt Concrete Plants,
     Iron and Steel Plants,...Volume 1.  Publication No. APTD-135a.
     Research Triangle Park, North Carolina,  p. 61.

Environmental Protection Agency.  1974a.  Background Information for New
     Source Performance Standards:  Primary Copper, Zinc, and Lead
     Smelters.  Volume 1:   Proposed Standards.  EPA-450/2-74-002a.
     Research Triangle Park, North Carolina,  pp.  6-1 to 6-139.

Environmental Protection Agency.  1974b.  Background Information for
     Standards of Performance:   Primary Aluminum Industry.  Volume 1:
     Proposed Standards.  EPA 450/2-74-020a.  Research Triangle Park,
     North Carolina. 97 p.

Environmental Protection Agency.  1974c.  Background Information for
     Standards of Performance:   Electric Submerged Arc Furnaces for
     Production of Ferroalloys.  Volume 1:  Proposed Standards.   EPA
     450/2-74-018a.  Research Triangle Park, North Carolina.  147 p.

Environmental Protection Agency.  1974d.  Background Information for
     Standards of Performance:   Electric Arc Furnaces in the Steel
     Industry.  Volume 1:   Proposed Standards.  EPA 450/2-74-017a.
     Research Triangle Park, North Carolina.  155 p.

Environmental Protection Agency.  1978.  Economic Impact Assessment for
     the National Ambient Air Quality Standard for Lead.  Office of Air
     Quality Planning and Standards.  Research Triangle Park, North
     Carolina,  p. 56.
                                    8-74

-------
43 Federal  Register  52952.   Occupational  Exposure to Lead Attachments to
      the  Preamble  for the  Final  Standard^   Occupational  Safety and
      Health Administration.   Washington,  D.C.   Office of the Federal
      Register.   November 21,  1978.

Hough, Ruth, Bureau  of Mines.  1981.   Telephone conversation with
      M. Buckwalter,  TRW.   January  71   Price information  for metallic
      mineral processing  concentrates.

Kurtz, H.,  U.S.  Bureau of  Mines.   1980.   Telephone conversation with
      M. Buckwalter,  TRW.   October  16.   Capital  costs for alumina plants.

Neveril,  R.  B.   1978.  Capital and Operating Costs of Selected Air
      Pollution Control Systems.  Gard,  Inc., Niles,  Illinois.
      EPA-450/5-80-002.

Peters, M.  S. and  K.  D.  Timmerhaus.  1968.   Plant Design and Economics
      for  Chemical  Engineers.  New  York, McGraw-Hill,,  p.  90-142.

Rathjen,  J., Bureau  of Mines.  1981.   Telephone conversation with
      M. BuckwaTter,  TRW.   January  7.   Price information  for metallic
      mineral processing  concentrates.

Singmaster, D. and S.  Breyer.  1973.   Air Pollution  Control  in the
      Primary Aluminum  Industry.  Contract No. CPA 70-21  for the
      Environmental Protection Agency.   Research Triangle Park,  North
      Carolina,   pp.  40 to  53.

Valerioti,  F., Ducon Company.  1979.   Telephone conversation with  J. Oatway,
      GCA Technology  Division.  October  22 and 24.  Capital  cost information
      of the Ducon W-4  Scrubber.

Weaver, J.  B.  1973.   Cost and Profitability Estimation.   In:   Chemical
      Engineer's  Handbook,  5th Edition.  Perry,  R.  H.  (ed.).   New York,
      McGraw-Hill,  p.  25-1 through 25-47.
                                   8-75

-------

-------
                              9.   ECONOMIC  IMPACT

 9.1   INDUSTRY CHARACTERIZATION
      As discussed  in Chapter  3, the products of the metallic mineral
 industries range from mineral concentrates to complex compounds to pure
 metals.  The metals included  in these  industries under discussion, along
 with  the product of each type of  processing plant, are listed in
 Table 9-1.  Because of the diversity within the industries, each metal
 will be treated separately in this profile.
      Unless otherwise noted, information on each metal was obtained
 from the Mineral Commodity Profiles and the Mineral Commodity Summaries
 (both published by the U.S. Bureau of Mines).   The specific references
 for these two sources are presented under the individual metal statistical
 tables.  Estimates for capacity for new growth were based on an annual
 survey of mine and plant expansions that appeared in the Engineering and
Mining Journal (January 1980) and on personal  communications with
 industry and U.S.  Bureau of Mines personnel.   The information provided
 in Section 8.1 (cost of control) and in Section 9.1 form the basis for
 formal analyses of the economic impact of regulatory alternatives on the
various metallic mineral  processing industries.   These analyses are
presented in Section 9.2.

-------
              Table 9-1.  METALLIC MINERAL PROCESSING PRODUCTS
     Metal
          Process product
Aluminum
Copper
Gold
Iron
Lead/Zinc
Molybdenum
Silver
Titani um/Zi rconi urn
  (sand-type ore)
Tungsten
Uranium
Alumina (aluminum oxide)
25 percent copper sulfide concentrate
Refined metal often combined with
  silver
Taconite pellets (^60 to 65 percent
  iron)
90 to 95 percent lead and zinc sulfide
  concentrates
90 to 95 percent molybdenum sulfide
  concentrate
Refined metal often combined with
  gold (dore)
95 percent ilmenite plus zircon concen-
  trate
65 percent tungsten oxide concentrate
Yellowcake (90+ percent, uranium oxide,
 ,U3°8>
                                    9-2

-------
9.1.1  Aluminum
     Aluminum is made from alumina which is produced when bauxite is
processed.  This chapter is concerned with the processing of bauxite
into alumina; the reduction of alumina .into aluminum has been covered
elsewhere (see Section 8.2).  The United States is the world's largest
consumer of aluminum, but domestic producers must depend on imports of
bauxite and alumina to meet over 90 percent of their demand for raw
material as shown in Table 9-2.  The major exporters of bauxite for use
in the U.S.  are Guinea, Jamaica, and Surinam.  Many bauxite mines are
captive operations owned by U.S. processers, and so the price data
provided by the U.S. Bureau of Mines in Table 9-2 can only be estimates.
     There are nine active bauxite processing operations in the
United States located primarily in the states of Texas and Louisiana
because of the proximity of this region to traditional sources of imported
bauxite (see Tables 9-3 and 9-4).   The processing plants are typically
part of large integrated companies.   Frequently the product of these
processing plants (alumina) is shipped to reduction plants in other
parts of the country which have cheaper or more abundant electrical
energy.  Eighty-eight percent of bauxite is used to produced aluminum
metal with the remainder used in refractories and/or chemicals and
abrasives (see Table 9-5).
     The domestic aluminum ore mining industry will expand at a very
slow rate and imports of aluminum ore and alumina will account for an
increasing share of the domestic market.   Two new bauxite/alumina pro-
cessing plants are projected to be built by 1985 with ore capacities of
140 and 270 Mg per hour.   These additions represent an annualized growth
rate of 2.1 percent for the bauxite/alumina processing capacity.   These
plants are expected to process bauxite containing approximately 22 percent
aluminum.
     Domestic aluminum production was approximately 5,300,000 Mg
(5,800,000. tons) in 1978 (see Table  9-6), exceeding every metal  except
iron.  The transportation,  packaging, construction, and aerospace
industries are increasing their use  of aluminum as a substitute for
                                 9-3

-------
steel (see Table 9-7).   Aluminum has many of the structural  qualities  of
steel but at the same time is much lighter.   These qualities make
aluminum particularly important to the transportation industry's effort
to increase fuel efficiency by making lighter vehicles.
     Possible substitutes for aluminum include wood in the construction
industry; plastics, titanium, steel, and graphite in transportation;
copper in the electrical industry; plastics, glass, and paper in the
container industry; plastics and steel in appliances; and steel, magne-
sium, titanium, copper-nickel alloys and other composites in machinery.
In the manufacturing process, however, substitution of materials often
necessitates the purchase or modification of equipment.   This not only
means that the substituted material must offer improvements  in cost and
performance, but that such a change most likely would occur  very slowly.
     The price of aluminum in constant 1976 dollars, shown in Table 9-8,
declined until 1974.  In constant 1976 dollars, the 1977 price was
identical to the 1954 price.
                                 9-4

-------
                  Table 9-2.  PRODUCTION PROFILE:  BAUXITE'
     Parameters
                  Year
                                 1974
           1975
      1976
      1977
      1978
Production:  Mine, 1000 Mg
  (1,000 tons) as bauxite

Imports of bauxite for con-
  sumption, 1,000 Mg (1,000
  tons) as bauxite

Imports of alumina, 1,000 Mg
  (1,000 tons) as alumina

Exports of bauxite, 1,000 Mg
  (1,000 tons) as bauxite

Exports of alumina, 1,000 Mg
  (1,000 tons) as alumina

Employment:  domestic bauxite
               mines
             alumina processing

Net import reliance  as a
  percent of apparent con-
  sumption

Price $ per Mg ($ per ton)
  of bauxite
  1,980   1,800   1,989   2,013   1,620
 (2,182) (1,984) (2,192) (2,218) (1,785)

 16,000  12,000  13,500  13,600  14,500
(17,632)(13,224)(14,877)(14,987)(15,979)
  3,290   3,182   3,288   3,760   4,000
 (3,626) (3,507) (3,623) (4,144) (4,408)
16
(18)
927
(1,022) 1
350
-
20
(22)
934
k. J *J £• •* J
350
-
15
(17)
1,050
(1,157)
350
-
26
(29)
856
(943)
350
-
23
(25)
878
(968)
325
7-8,000
     92
91
91
91
93
    5-15    5-15    5-15    5-15    5-15
   (5-14)   (5-14)  (5-14)   (5-14)   (5-14)
dU.S.  Bureau of Mines, 1980.
 Net import reliance = imports-exports+adjustments for Government and
industry stock changes.
                                    9-5

-------
               Table 9-3.   BAUXITE INDUSTRY CHARACTERISTICS
Number of leading companies
Number of active operations
Value of processing plant output
Percent of output controlled by leading
  companies
Major bauxite processing states

Ratio of bauxite to aluminum metal
Ratio of alumina to aluminum metal
3
9
$482.8 million
86
Texas,
Louisiana
4.5
2.0
                                    9-6

-------




















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-------
                    Table 9-5.   PRODUCT USES:   BAUXITE0
     Product uses
                                               Percent
     Aluminum metal

     Refractories,  chemicals,  abrasives,
       etc.
88


12
aU.S.  Bureau of Mines,  1980.
                                   9-8

-------
                 Table 9-6.  PRODUCTION PROFILE:  ALUMINUM11
     Parameters
               Year
                                1974
        1975
1976
1977
1978
Production 1,000 Mg (1,000 tons)
  as metal
  Primary (reduction plants)   4,448
                              (4,902)
  Secondary (from old scrap)
Imports for consumption
  1,000 Mg (1,000 tons) as
  metal
       3,519   3,856   4,118   4,355
      (3,878) (4,249) (4,538) (4,799)
 276     306     371     455     499
(304)   (337)   (409)   (501)   (550)

 571     499     679     758     998
(629)   (550)   (748)   (835)  (1,100)
Exports 1,000 Mg (1,000 tons)    475
  as metal                      (523)

Net import reliance as a
  percent of apparent con-
  sumption                         4

Employment:

  Primary reduction0          24,000

  Secondary smelter            4,100
         399     439     373     435
        (440)   (484)   (411)   (479)
                                  10
      19,000  20,800  22,000  23,000

       4,000   4,200   4,200   4,300
 U.S.  Bureau of Mines, 1980.
 Net imports reliance = imports-exports+adjustments for Government and
industry stock changes.
 Estimate.
                                  9-9

-------
                 Table  9-7.   PRODUCTS  USES:   ALUMINUM METALC
     Product uses
Percent
     Building
     Packagi ng
     Transportation
     Electrical
     Consumer durables
     Other
  25
  22
  23
  11
   8
  11
*U.S.  Bureau of Mines,  1980.
                                   9-10

-------
                    Table 9-8.  PRICE HISTORY:  ALUMINUM"
Year
Actual prices
Based on constant
  1976 dollars

1954
1955
1956
1957
1958
1959
1960
1961
1962
1963
1964
1965
1966
1967
1968
1969
1970
1971
1972
1973
1974
1975
1976
1977
Oct.b
1979
$/kg
0.49
0.53
0.57
0.62
0.60
0.60
0.57
0.57
0.53
0.51
0.53
0.55
0.55
0.55
0.57
0.60
0.64
0.64
0.57
0.55
0.75
0.88
0.99
1.15

1.43
$/lb
0.22
0.24
0.25
0.28
0.27
0.27
0.26
0.26
0.24
0.23
0.24
0.25
0.25
0.25
0.26
0.27
0.29
0.29
0.26
0.25
0.34
0.40
0.45
0.52

0.65
$/kg
1.08
1.17
1.21
1.28
1.21
1.19
1.12
1.10
1.01
0.95
0.97
0.99
0.97
0.93
0.93
0.93
0.95
0.88
0.77
0.71
0.86
0.93
0.99
1.08

"
$/lb
0.49
0.53
0.56
0.58
0.55
0.54
0.51
0.50
0.46
0.43
0.44
0.45
0.44
0.42
0.42
0.42
0.43
0.40
0.35
0.32
0.39
0.42
0.45
0.49

_ _
 Average annual  price of aluminum metal  from Stamper and Kurtz (1978).

'Average price for October from Engineering and Mining Journal (1979).
                                   9-11

-------
9.1.2  Copper
     In 1978, the United States was the world's leading producer and
consumer of copper.  Many copper producers are highly integrated with
all operations from mining through smelting and fabrication owned by one
corporation.  At many plants all operations from processing of ore
through the fabrication of final products are located on the mine site.
As shown in Table 9-9, approximately 67 percent of the domestic copper
supply comes from domestic mines, 21 percent from old scrap, and
12 percent from imports.  As shown in Table 9-10, the copper market has
undergone wide price fluctuations between 1973 and 1979.
     Product uses of copper are profiled in Table 9-11.  Over one-half
of domestic consumption went into electrical applications such as motors,
generators, power distribution, industrial controls, communications
equipment, and residential wiring.  Non-electrical applications include
roofing, plumbing, decorative items, heat exchangers, shell casings,
instruments, household utensils, jewelry, and coinage.
     Although copper is the preferred material for numerous uses,
aluminum, plastics, steel, and other materials are possible substitutes
in some cases.  Aluminum has replaced copper to some degree in insulated
power cable and, to a great extent, in bare conductor applications.
Aluminum may also replace copper in the manufacture of automobile
radiators.
     As summarized in Table 9-12, the eight leading copper companies
control approximately three-quarters of the total output.  Most companies
are highly integrated with operations from mining through smelting and
refined metal production often located at one site.  Table 9-13 lists 41
copper processing plants, located primarily in Arizona, New Mexico,
Utah, and Nevada.
     The demand for copper is expected to increase at an annual rate of
approximately 3 percent through 1985.  Ore capacity is expected to
increase at an annualized rate of 1 percent through 1985.  New
facilities are projected to include one 540 and one 140 Mg per hour
plant.  The trend  in the industry is to utilize lower grade ore as
richer deposits become exhausted.  Ore grades for larger new processing
plants will probably average from 0.4 to 0.5 percent copper while
smaller operations will be tailored to less extensive but richer

                                 9-12

-------
 deposits  (1 to  2  percent copper).   Both  new plants  were  assumed  to
 process 0.45 percent copper ore.   The  recovery of other  minerals, such
 as  molybdenum,  zinc, silver,  and  uranium,  will  continue  to  play  a
 significant role  in the profitability  of some operations.
      The  development of the copper deposits in Minnesota will
 significantly increase the domestic supply of nickel  with the  recovery
 of  this metal as  a byproduct from new  copper operations.  The
 recoverable nickel reserves in these operations are estimated  at
 5 million tons  of metal.   The deposits vary in concentration from 0.3 to
 over 0.6  percent  copper and from  0.1 to  0.2 percent nickel.
      AMAX has conducted active exploration and has  tentative plans  for  a
 pilot plant operation in Minnesota.  Commercial development is possible
 before 1990.  A single economical  commercial development is expected to
 require 20 million tons of ore per year  (2,100 Mg/hour)  from an  open pit
 operation processing ore at 0.45  percent copper and 0.15 percent nickel.
 These operations  are expected to  be relatively high cost operations due
 to  the very hard  gangue from which the mineral  must be recovered (Veith,
 1980).  Because the nickel concentrations are so low, nickel could  not
 be  economically recovered except  as a  byproduct of  copper in these
 operations.   For  this reason separate  analyses of the impact of  emission
 control alternatives on the nickel industry was not performed.   Economic
 impacts on copper-nickel operations would be less severe than  on
 operations recovering only copper.
      Demand for nickel is expected to  increase at 3 percent per  year
 through 1985.  The United States  imports most of its nickel from Canada.
 Vital to  the iron and steel industry,  nickel's greatest  value  is in
 alloys with other elements, where it provides strength and  corrosion
 resistance.   These alloys include stainless steel,  superalloys,
 nickel-copper alloys, and copper-nickel  alloys.  The domestic  nickel ore
 processing industry currently consists of one integrated processing
 plant located in  Oregon and operated by  Hanna Mining Company.  AMAX has
 a nickel  refinery located in Louisiana,  but it produces  nickel metal
. from imported intermediate (matte) materials.
                                  9-13

-------
                 Table 9-9.  PRODUCTION PROFILE:  COPPERC
     Parameters
                  Year
                                  1974
          1975
        1976
1977
1978
Production:  Mine 1,000 Mg
  (1,000 tons) as metal

Refined copper: 1,000 Mg
  (1,000 tons) as metal

  Primary


  Secondary
 1,449   1,282   1,457   1,364   1,358
(1,597) (1,413) (1,606) (1,503) (1,497)
 1,501   1,309   1,396   1,357   1,449
(1,654) (1,443) (1,538) (1,495) (1,597)

   451     312     340     349     420
  (497)   (344)   (375)   (385)   (463)
Imports for consumption
  1,000 Mg (1,000 tons) as metal:

  Total
  Refined


Exports 1,000 Mg (1,000 tons) as metal

  Total
573
(631)
284
(313)
246
(271)
130
(143)
425
(468)
346
(381)
396
(436)
351
(387)
532
(586)
403
(444)
  Ref i tied
Employment:  mine and mill
                   L
Net import reliance  as a
  percent of apparent con-
  sumption
   173
  (191)

   115
  (127)
 212     156     113     178
(234)   (172)   (125)   (196)
 156     102
(172)   (112)
  47      92
 (52)   (101)
36,300  33,500  29,700  29,400  26,400
    20
          12
  13
  20
aU.S. Bureau of Mines, 1980.
bNet import reliance = imports-expofts+adjustments for Government and
industry stock changes.
°Net exports.
                                   9-14

-------
                   Table 9-10.  PRICE HISTORY:  COPPERC
Year
Actual prices
Based on constant
  1978 dollars

1958
1959
1960
1961
1962
1963
1964
1965
1966
1967
1968
1969
1970
1971
1972
1973
1974
1975
1976
1977
1978.
1979°
1979C
$/kg
58.0
67.7
70.8
66.1
67.9
67.9
71.9
78.0
80.7
85.1
93.0
105.6
128.3
114.6
112.9
131.2
170.4
141.5
153.4
147.3
146.6
199.5
218.5

-------
                    Table 9-11.   PRODUCT USES:   COPPER

Product uses
Electrical
Construction
Industrial machinery
Transportation
Other
1978
(percent)
58
19
9
8
6
1979
(percent)
58
18
9
9
6
aU.S. Bureau of Mines, 1980.
              Table 9-12.  INDUSTRY CHARACTERISTICS:   COPPER
Number of leading companies

Number of active operations
Percent, of capacity controlled by
  leading companies

Value of processing plant output (as
  95 percent concentrate)

Major processing states
Ratio of ore to product
8

34 (6 temporarily
  inactive, 1 under
  construction)
76
$220.8 million

Arizona, Nevada, Utah,
  New Mexico

Range:  200 - 250
                                   9-16

-------



























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  • -------
    9.1.3  Gold
         Gold's unique position in world history and in international
    financial markets has made the metal as valuable for an investment as
    for an industrial metallic mineral.   Table 9-14 summarizes the product
    uses of gold.  Gold's properties of chemical inertness, malleability,
    reflectiveness, and thermal and electrical conductivity are the basis
    for its industrial applications and use in jewelry and dentistry.   The
    electronics industry (which is the major industrial consumer of gold)
    is, however, decreasing their use of gold due to its current high price.
    As shown in Table 9-15, the price of gold has risen dramatically from
    $1.17 per gram ($36.41 per troy ounce) in 1970 to a high of $25.72 per
    gram ($800 per troy ounce) in January 1980.
         The United States mines and reclaims from scrap less than one-half
    the gold required by domestic fabricators (see Table 9-16).   From 1973
    to 1978, imported bullion came primarily from Canada, Switzerland, and
    the USSR.
         Although gold use can be reduced by more efficient use and
    substitution, any substitute brings with it an impairment in performance.
    Platinum and palladium can be substituted in some instances, but
    consumers prefer gold.  Silver has some of gold's qualities but has less
    resistance to corrosion.  A titanium and chrome-based alloy has been
    developed for dental applications, but it lacks gold's malleability.
         Table 9-17 presents industry characteristics and shows that the
    industry is dominated by four major companies.  The gold industry is
    located primarily in Nevada, California, Colorado, South Dakota, and
    Washington.   Table 9-18 lists 20 domestic gold ore processing plants.
         In the United States, about 60 percent of domestic production comes
    from primary gold ores, with the remainder produced as a byproduct of
    copper and other base metals.  Domestic lode gold mining has, in the
    past, been directed towards grades of ores having 0.3 troy ounces of
    gold per ton of ore or greater, but recent technology and higher gold
    prices have combined to permit exploitation of much lower grade ores in
    the range of 0.05 to 0.1 troy ounces per ton.
         The demand for gold is expected to increase at an annual rate of
    2.7 percent through 1985.  If gold prices remain high, production is
                                     9-22
    

    -------
    likely to decline temporarily, because high price levels allow mining of
    a greater proportion of lower grade ores.   On the other hand,  higher
    price levels should also encourage the expansion of existing mines and
    the opening of additional mines (Etheridge, 1980).   Mine production and
    growth capacity are difficult to estimate through 1985.   Two new plants
    are projected to be built before 1985; one plant at 68 Mg per hour
    capacity and one plant at 140 Mg per hour capacity.   An ore grade of 0.2
    troy ounces per ton of ore was assumed for these new plants.
                                     9-23
    

    -------
                        Table 9~14.  PRODUCT USES:  GOLDC
    
    Product uses
    Jewelry and arts
    Industrial (mainly electronic)
    Dental
    Small bars, etc., mainly for
    investment
    1978
    (percent)
    56
    27
    16
    1
    1979
    (percent)
    58
    28
    13
    1
    U.S. Bureau of Mines, 1980.
                                      9-24
    

    -------
                        Table 9-15.  PRICE HISTORY:  GOLD'
    Year
    Actual prices
                                                        Based on constant
                                                          1977 dollars
    
    1956
    1957
    1958
    1959
    1960
    1961
    1962
    1963
    1964
    1965
    1966
    1967
    1968
    1969
    1970
    1971
    1972
    1973
    1974
    1975
    1976
    1977,
    1978°
    1979°
    $/gram
    1.13
    1.13
    1.13
    1.13
    1.13
    1.13
    1.13
    1.13
    1.13
    1.13
    1.13
    1.13
    1.26
    1.33
    1.17
    1.33
    1.88
    3.14
    5.14
    5.19
    4.03
    4.77
    5.92
    12.62
    $/troy oz
    35.00
    35.00
    35.00
    35.00
    35.00
    35.00
    35.00
    35.00
    35.00
    35.00
    35.00
    35.00
    39.26
    41.51
    36.41
    41.25
    58.60
    97.81
    159.74
    161.49
    125.32
    148.31
    184.00
    392.73
    $/gram
    2.47
    2.38
    3.32
    2.28
    2.24
    2.21
    2.19
    2.16
    2.13
    2.09
    2.04
    1.97
    2.12
    2.14
    1.78
    1.93
    2.66
    4.20
    6.23
    5.76
    4.25
    4.77
    --
    
    $/troy oz
    76.70
    73.91
    72.08
    70.88
    69.82
    68.89
    68.09
    67.22
    66.27
    65.06
    63.30
    61.29
    66.08
    66.66
    55.46
    60.09
    82.58
    130.52
    193.74
    179.17
    132.30
    148. 31
    --
    
    aAverage annual price of gold metal from Butterman (1978).
    
     First 6 months.
    cAverage price for October from Engineering and Mining Journal (1979).
                                        9-25
    

    -------
                      Table 9-16.  PRODUCTION PROFILE:  GOLD0
         Parameters
                      Year
                                     1974
              1975
          1976
          1977
          1978
    Production 1,000 kg (1,000 IDS) as metal
      Mi ne
    
    
      Refinery:
    
        New (domestic as metal)
      35.1    32.7
     (77.4)  (72.1)
      31.7    33.9
     (69.9)  (74.7)
        Secondary (including toll    59.1    84.0
          as metal)
    (130.3) (185.2)
    General imports 1,000 kg (1,000  82.4    82.7
      IDS) as metal
    
    Exports 1,000 kg (1,000
      IDS) as metal
    
    Employment:  mine and mill
    
    Net import reliance  as a
      percent of apparent con-
      sumption
    (181.7) (182.3)
    
      17.7    83.7
     (39.0) (184.5)
          32.7
         (72.1)
          29.5
         (65.0)
    
          77.8
        (171.5)
    
          82.7
        (182.3)
    
          89.6
        (197.5)
          34.2    30.2
         (75.4)  (66.6)
          29.9    31.1
         (65.9)  (68.6)
    
          76.2    96.4
        (168.0) (212.5)
    
         138.4   145.6
        (305.1) (321.0)
    
         218.0   176.0
        (480.6) (388.0)
     2,600   3,000   3,200   3,200   3,200
        63
    52
    60
    61
    54
     U.S. Bureau of Mines, 1980.
     Net import reliance = imports-exports+adjustments for Government and
    industry stock changes.
                                       9-26
    

    -------
                   Table 9-17.   INDUSTRY CHARACTERISTICS:   GOLD
    Number of leading companies
    
    Number of active operations
    
    Percent of capacity controlled by
      leading companies
    
    Value of processing plant output (as
      metal)
    
    Major processing states
    
    
    Ratio of ore to product
    17 (3 inactive)
    70
    $415.4 million
    
    Nevada, South Dakota,
      Utah, Arizona
    
    Range:  100,000 -
      640,000
                                       9-27
    

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    9.1.4  Iron Ore
         Iron is the most widely used metal in the world.  Although the
    United States is the fourth largest producer of iron ore, imports have
    grown from less than 5 percent of demand in 1953 to about one-third of
    the total requirement in 1977 (see Table 9-19).  Over one-half of the
    1977 imports came from mines owned, operated, or partially owned by
    United States mining and steel companies.
         The domestic iron ore mining and processing industries are
    dominated by large, integrated steel companies.  As shown in Tables 9-20
    and 9-21, about 85 percent of total iron ore output in 1977 was produced
    by 18 out of 45 mines, operated by 8 out of 34 companies.  Table 9-21
    lists 41 iron ore processing plants.  Most are located in Minnesota or
    Michigan.
         Almost all iron ore mined today is beneficiated before shipment.
    After beneficiation, iron ore particles are usually agglomerated before
    use in blast furnaces.  Agglomeration usually involves sintering and
    pelletizing.  The average grade of crude ore (iron ore in its natural
    state) is 36 percent and the iron content of the final product of mining
    and beneficiation operations is typically raised to between 60 and
    65 percent.
         Table 9-22 lists product uses of iron and steel..  In some cases
    aluminum may take iron's place as a structural  support,  as a packaging
    material, and in the transportation industry.   Plastics  and other
    polymeric materials have also replaced some uses of steel in the
    automobile industry due to the recent emphasis  on lighter, more
    fuel-efficent cars.
         Table 9-23 presents the price history of iron.   Prices have shown a
    steady rise since the mid-seventies.
         The expansion of capacity for the iron ore processing industry is
    directly related to the financial  condition and planned  production
    increases of the steel industry.   The steel industry is  expected to
    maintain a good growth rate through 1985,  with  demand for iron increasing
    at an annual  rate of 2.5 percent.   Two new iron ore processing plants
    are projected between now and 1985,  one at 1,100 Mg per  hour and one at
    2,200 Mg per hour.   Crude ore grades were assumed to be  36 percent as
    iron.
                                     9-31
    

    -------
                    Table 9-19.   PRODUCTION PROFILE:   IRON ORE0
         Parameters
                  Year
                                     1974    1975
                  1976
                  1977
                  1978
    Production million Mg (million   85.8    80.2    81.3    56.7    81.8
      tons) as metal                (94.6)  (88.4)  (89.6)  (62.5)  (90.1)
    
    Imports for consumption million  48.8    47.7    45.1    38.5    33.5
      Mg (million tons) as metal    (53.8)  (52.6)  (49.7)  (42.4)  (36.9)
    
    Exports million Mg (million       2.3     2.5     2.9     2.1     3.8
      tons) as metal                 (2.5)   (2.8)   (3.2)   (2.3)   (4.2)
    Employment:  mine and con-
      centrating plant (average)   20,000  19,900  20,500  20,200  19,700
    Net import reliance  as a
      percent of apparent con-
      sumption (iron in ore)
    37
    39
    31
    48
    29
    aU.S. Bureau of Mines, 1980.
    bNet import reliance = imports-exports+adjustments for Government and
    industry stock changes.
                                       9-32
    

    -------
                   Table 9-20.  INDUSTRY CHARACTERISTICS:   IRON
    Number of leading companies
    Number of active operations
    Percent of capacity controlled by
      leading companies
    Value of processing plant output
      (as taconite pellets)
    Major processing states
    Ratio of ore to product
     8
    36 (5 temporarily
      inactive)
    85
    
    $88.1 million
    Minnesota, Michigan
    2.8
                                      9-33
    

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    -------
                         Table 9-22.  PRODUCT USES:  IRONC
        Product uses
      1979
    (percent)
    Transportation
    Construction
    Machinery
    Oil and gas
    Cans and containers
       31
       27
       20
        7
        6
    aU.S. Bureau of Mines, 1980.
                                        9-40
    

    -------
                     Table 9-23.  PRICE HISTORY:   IRON  IN ORE
                                                             a
    Year
    Actual price
    Based on constant
      1978 dollars
    
    1957
    1958
    1959
    1960
    1961
    1962
    1963
    1964
    1965
    1966
    1967
    1968
    1969
    1970
    1971
    1972
    1973
    1974
    1975
    1976
    1977°
    1979C
    $/Mg
    15.98
    15.87
    16.09
    15.98
    16.20
    15.87
    16.09
    16.42
    16.42
    16.42
    16.87
    17.09
    17.20
    18.08
    18.96
    19.62
    20.72
    26.34
    34.50
    38.58
    40.67
    41.20
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    14.50
    14.40
    14.60
    14. 50
    14.70
    14.40
    14.60
    14.90
    14.90
    14.90
    15.30
    15.50
    15.60
    16.40
    17.20
    17.80
    18.80
    23.90
    31.30
    35.00
    36.90
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    32.85
    32.19
    31.97
    31.20
    31.31
    30.09
    30.09
    30.20
    29.54
    28. 66
    28.55
    27.67
    26.57
    26.46
    26.46
    25.23
    26.23
    30.42
    36.27
    38. 58
    42.99
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    29.00
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    28.40
    27.30
    27.30
    27.40
    26.80
    26.00
    25.90
    25.10
    24.10
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    24.00
    23.80
    23.80
    27.60
    32.90
    35.00
    39.00
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     Average annual  price of iron pellets from Klinger (1978).
    ^Preliminary.
    
    "Average price for October from Engineering and Mining Journal  (1979).
                                       9-41
    

    -------
    9.1.5  Lead
         The United States is both the leading producer and consumer of
    lead.  As shown in Table 9-24, about 40 percent of the lead consumed is
    reclaimed from old scrap materials, chiefly storage batteries.
    Approximately 14 percent of the United States lead supply is imported.
         Table 9-25 summarizes the product uses of lead.   The largest use of
    lead is for lead storage batteries, which are used in the transportation
    and communication industries as well as by electric utilities.   Lead is
    also used as an anti-knock additive in gasoline, although this  use is
    decreasing because of the environmental regulations reducing lead in all
    types of gasoline and eliminating lead from fuel for cars equipped with
    catalytic converters.  In construction, lead is used as a sound barrier
    and a radiation shield.  Lead paint is used to protect steel in highway
    and building construction and for safety markings on highways.   Lead is
    also used for cables, ammunition, packaging, glass porcelain enamel, and
    ceramic glazes.  The use of lead in some products has been reduced due
    to the possibility of lead poisoning and potentially adverse environmental
    impacts.
         Alternative materials are available for use in batteries,  but they
    either are limited in supply, cost more than lead, or do, not have the
    electrical characteristics necessary to meet the volume of automotive
    and industrial power requirements.  New anti-knock materials for gasoline
    are currently under development and may eventually replace lead.  Lead
    has been replaced in exterior house paint by titanium and zinc  pigments.
    Unless extreme corrosion is a problem, underground cables can be made of
    polyethylene and combinations of metallic and organic materials.
    Although other materials may sometimes be substituted for lead  (e.g., in
    ammunition and in containers) the growth of lead use in batteries and in
    newly developing applications assures its continued long-term growth.
    As shown in Table 9-26, the prices in constant dollars have fluctuated
    and were actually less in 1976 than in 1954.
         The lead processing industry characteristics are summarized in
    Table 9-27.  Processing plants whose primary products are lead and zinc
    concentrates are listed in Table 9-28.  Domestic production of lead
    continues to come chiefly from ores mined primarily for their lead
                                     9-42
    

    -------
     content;  additional  lead  is  derived  from  ores  in which  lead and zinc are
     comparably  valued  as  coproducts.   Lead  is also recovered as a byproduct
     from  ores mined  for  copper,  gold,  silver,  zinc, or  fluorine. • Profitable
     processing  of  the  complex ores  of  the Rocky Mountain areas is particularly
     dependent on the aggregate value of  the lead,  zinc, silver, and gold
     content rather than  the value of any one  metal.  In addition to lead,
     the principal  metals  recovered  in  processing lead ores  and concentrates
     are copper, zinc,  silver, antimony,  tellurium, gold, and bismuth.
     Significant quantities of sulfur,  as sulfuric  acid, also are recovered
     as byproducts  of lead production.
         The  average grade of Missouri ore is 6 percent lead and 1 percent
     zinc, while the  more complex vein  ores of Idaho and the Rocky Mountain
     area average about 3 percent lead  and 1 percent zinc.
         Demand for  lead is expected to  increase at an annual  rate of 1 to
     2 percent through 1985.   Growth in processing capacity between 1980 and
     1985 is projected to include a 540 Mg per hour plant and two  270 Mg per
     hour plants.  Industry growth is expected primarily in Missouri  and
    Tennessee and ore grades for new plants  are presumed to be  4.5 percent
     lead and 1 percent zinc.
                                    9-43
    

    -------
                     Table 9-24.   PRODUCTION PROFILE:   LEADC
    
    Parameters
    Production 1,000 Mg (1,000 tons)
    Mine
    Ref i nery
    Secondary
    Imports for consumption 1,000 Mg
    (1,000 tons) as metal
    Ores, concentrates, and
    bullion
    Pigs and bars
    Exports 1,000 Mg (1,000 tons)
    as metal
    Employment:
    Mine, and mill
    Smelters and refineries
    Net import reliance0 as
    percent of apparent con-
    sumption
    
    1974
    as metal
    602
    (663)
    620
    (683)
    634
    (699)
    
    85
    (94)
    109
    (120)
    110
    (121)
    
    4,800
    2,400
    19
    
    1975
    
    563
    (620)
    579
    (638)
    597
    (658)
    
    80
    (88)
    96
    (106)
    64
    (71)
    
    4,600
    2,400
    11
    Year
    1976
    
    553
    (609)
    598
    (659)
    660
    (727)
    
    69
    (76)
    134
    (148)
    48
    (53)
    
    4,700
    2,400
    15
    
    1977
    
    537
    (592)
    552
    (608)
    757
    (834)
    
    73
    (80)
    237
    (261)
    86
    (95)
    
    4,600
    2,400
    13
    
    1978
    
    530
    (584)
    568
    (626)
    769
    (847)
    
    66
    (73)
    225
    (248)
    126
    (139)
    
    4,600
    2,400
    11
    aU.S.  Bureau of Mines, 1980.
    blncludes all lead and/or lead-zinc processing units.
    cNet import reliance = imports-exports+adjustments for
    industry stocks.
    Government and
                                       9-44
    

    -------
                         Table  9-25.   PRODUCT USES:   LEAD*
    
    Product uses
    Transportation:
    Batteries
    Gasoline additives
    Electrical
    Paints
    Ammunition
    Construction
    Other
    1978
    (percent)
    
    51
    15
    8
    6
    4
    3
    13
    1979
    (percent)
    
    61
    12
    2
    6
    4
    3
    12
    U.S.  Bureau of Mines, 1980.
                                      9-45
    

    -------
                        Table 9-26.   PRICE HISTORY:   LEADC
    Year
    Actual price
     Based on constant
       1976 dollars
    
    -------
                   Table 9-27.  INDUSTRY CHARACTERISTICS:  LEAD
    Number of leading companies (lead/zinc)
    
    Number of active operations (lead/zinc)
    
    
    Percent of capacity controlled by leading
      companies
    
    Value of processing plant output (as
      95 percent ZnS+PbS concentrate)
    
    Major processing states
    Ratio of ore to product
    8
    
    35 (11 temporarily
      inactive)
    85
    $86.9 million
    
    Missouri, Idaho,
      Colorado, Utah,
      New Jersey
    
    Range:   16 - 33
                                      9-47
    

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    -------
     9.1.6  Molybdenum
          The United States is the world's leading producer of molybdenum
     and, as shown in Table 9-29, is a net exporter of the metal.   About
     70 percent of domestic consumption goes to the production of molybdenum-
     containing steels.   Molybdenum in steel improves steel's hardness and
     resistance to temper embrittlement, abrasion, and corrosion.   The steels
     are used in all major segments of industry.   As shown in Table 9-30,
     molybdenum is also used in lubricants, catalysts, and pigments.
          Historically,  there has been little incentive to substitute for
     molybdenum because the price has been low.   As shown in Table 9-31,
     however,  the price increased substantially during the middle  to  late
     seventies leading to an increased interest in alternatives.   A number of
     alternative materials are available,  but their use may result in impaired
     performance or a cost disadvantage.   These materials include  boron,
     chromium,  manganese, and nickel,  all  of which can be used in  steel.
     Molybdenum-containing steel  could occasionally be replaced by plastics
     and ceramics.   Tungsten,  tantalum,  and graphite may be substituted  in
     various other areas.   The domestic  availability of molybdenum, plus  the
     fact that  it represents only a small  percentage of the composition of
     many steels,  tends  to discourage  most substitution efforts.
          The molybdenum ore processing  industry  is  dominated  by the  Climax
     Division of AMAX, Incorporated, which controls  over 80 percent of the
     total domestic  processing capacity  (see Tables  9-31 and 9-33).   The
     company opened  the  Henderson Mine in  Colorado during 1976  and expects
     the  mine's  output to  reach 23,000 Mg  (25,000 tons)  of  metal per  year  by
     1980.  Duval Copper and  Kennecott Copper, which  recover molybdenum from
     their copper mining operations, are also large producers of the  metal.
     They are listed  in  Table  9-13 with the copper processors.
         Approximately  70 percent of molybdenum is recovered from molybdenum
     ores, principally low grade  deposits  of the mineral molybdenite.   Ore
     grades range from 0.2 to  0.5 percent  as Mo$2, representing ore-to-
     product ratios of 500 and 200, respectively.  The remainder of the
     molybdenum supply is obtained as a byproduct from copper, tungsten,  or
     uranium processing.   In some cases the recovery of molybdenum from
    copper processing significantly improves the profitability of these
    operations.
                                     9-53
    

    -------
         The demand for molybdenum is expected to increase at an annual  rate
    of approximately 5 percent through 1985.  The growth in processing
    capacity is expected to include construction of one 270 Mg per hour
    plant and two 1100 Mg per hour plants by 1985.  Ore grades of 0.4 percent
    were assumed for these plants.
                                      9-54
    

    -------
                   Table 9-29:   PRODUCTION  PROFILE:   MOLYBDENUM6
    
    Parameters
    Year
    1974
    Production: mine 1,000
    (1,000 tons) as metal
    Imports for consumption
    centrate 1,000 Mg (1,
    as metal
    Mg
    
    , con-
    000 tons)
    
    Exports, molybdenum concentrate
    and oxide 1,000 Mg (1
    ,000
    50.
    (56.
    0.
    (0.
    
    35.
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    8
    0)
    1
    1)
    
    7
    3)
    1975
    48.
    (53.
    1.
    (1.
    
    28.
    (31.
    1
    0)
    2
    3)
    
    4
    3)
    1976
    51.
    (56.
    0.
    (1.
    
    28.
    (31.
    4
    6)
    9
    0)
    
    3
    2)
    1977
    55.
    (61.
    0.
    (1.
    
    29.
    (32.
    5
    2)
    9
    0)
    
    8
    8)
    1978
    59.
    (66.
    1.
    (1.
    
    31.
    (34.
    9
    0)
    2
    3)
    
    4
    6)
      tons)
    
    Employment:
    
      Mine and mill recovering
        molybdenum as the principal
        product                     2,600
    
    Net import reliance  as a
      percent of apparent con-
      sumption                          c
    2,700   3,700   4,300   4,500
     U.S. Bureau of Mines, 1980.
    
     Net import reliance = imports-exports+adjustments for Government and
    industry stocks.
    £
     Net exporter.
                                       9-55
    

    -------
    Table 9-30.  PRODUCT USES:  MOLYBDENUM*
    
    Product uses
    Transportation
    Machinery
    Oil and gas industry
    Chemicals
    Electrical
    Other
    1978
    (percent)
    21
    34
    15
    12
    8
    10
    1979
    (percent)
    22
    32
    17
    13
    8
    8
    aU.S. Bureau of Mines', 1980.
                      9-56
    

    -------
                     Table 9-31.  PRICE HISTORY:  MOLYBDENUM'
    
    Year
    1954
    1955
    1956
    1957
    1958
    1959
    1960
    1961
    1962
    1963
    1964
    1965
    1966
    1967
    1968
    1969
    1970
    1971
    1972
    1973
    1974
    1975
    1976
    1977
    Oct.b
    1979
    Actual
    $/kg
    2.31
    2.43
    2.60
    2.60
    2.76
    2.76
    2.76
    3.09
    3.09
    3.09
    3.42
    3.42
    3.42
    3.57
    3.57
    3.79
    3.79
    3.79
    3.79
    3.79
    4.45
    5.47
    6.48
    8.11
    
    19.48
    prices
    $/lb
    1.05
    1.10
    1.18
    1.18
    1.25
    1.25
    1.25
    1.40
    1.40
    1.40
    1.55
    1.55
    1.55
    1.62
    1.62
    1.72
    1.72
    1.72
    1.72
    1.72
    2.02
    2.48
    2.94
    3.68
    
    8.84
    Based
    1977
    $/kg
    5.49
    5.62
    5.86
    5.67
    5. .91
    5.78
    5.69
    6.31
    6.19
    6.11
    6.66
    6.50
    6.31
    6.39
    6.13
    6.19
    5.89
    5.60
    5.38
    5.07
    5.45
    6.08
    6.86
    8.11
    
    ""
    on constant
    dollars
    $/lb
    2.49
    2.55
    2.66
    2.57
    2.68
    2.62
    2.58
    2.86
    2.81
    2.77
    3.02
    2.95
    2.86
    2.90
    2.78
    2.81
    2.67
    2.54
    2.44
    2.30
    2.47
    2.76
    3.11
    3.68
    
    ""
    aAverage annual price per pound of molybdenum contained in
     concentrate (95% MoS2) from Kummer (1979).
     Average price for October from Engineering and Mining Journal (1979).
                                       9-57
    

    -------
                Table 9-32.   INDUSTRY CHARACTERISTICS:   MOLYBDENUM
    Number of leading companies
    Number of active operations
    Percent of capacity controlled by
      leading companies
    Value of processing plant output (as
      95 percent MoS2 concentrate)
    Major processing states
    Ratio of ore to product
    2
    3
    
    Not Available
    
    $133.9 million
    Colorado, New Mexico
    Range:  200 - 500
                                       9-58
    

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    9.1.7  Silver
         Silver, like gold, is valued both as an investment property and as
    an industrial metallic mineral.   As shown in Table 9-34, the photographic
    industry is the major consumer of silver, using 38 percent of the
    domestic supply in 1978.  Jewelry, arts and crafts, batteries, and
    electrical and electronic components are the other major use categories
    for silver.  The qualities that make silver valuable in industry are its
    superior thermal and electrical  conductivity; high reflectivity,
    malleability and ductility; and corrosion resistance.
         As a result of the silver price boom in 1979 (see Table 9-35),
    substitutes for silver should become more prevalent.  Stainless steel is
    used in the manufacture of flatware; aluminum and rhodium can replace
    silver in mirrors; and tantalum may be substituted in surgical plates,
    pins, and sutures.  Many countries are making coins from cupronickel,
    cuprozinc, nickel, and aluminum.  Substitutes for silver in the photo-
    graphic development process are being investigated, but to date, these
    efforts have not been successful.
         As shown in Table 9-36, the United States imports 45 percent of its
    silver while producing 12 percent of the world's supply.  There are  12
    processing plants whose primary product is silver located in Idaho,
    Colorado, and Montana (see Tables 9-37 and 9-38).
         Silver ores typically contain from 1 to 25 troy ounces of silver
    per ton of ore.  A recently developed mine contains 2.5 to 5.0 troy
    ounces per ton (Carter, 1978).  The recovery of gold and other metals in
    the processing of silver ore significantly added to the profitability of
    several operations.
         Demand for silver  in the United States was forecasted in 1978 to
    increase at an annual rate of around 3 percent through 1985.  A revised
    estimate taking into account the unanticipated rise in silver's price is
    not yet available.  Growth in processing capacity is projected to include
    two 45 Mg per hour plants and one 140 Mg per hour plant by 1985.  These
    plants are assumed to process ore containing 5 troy ounces of silver per
    ton of ore.
                                     9-60
    

    -------
                       Table 9-34.  PRODUCT USES:  SILVER0
        Product uses
      1978
    (percent)
      1979
    (percent)
        Photography
        Electrical and electronic
          components
        Sterlingware and electroplated
          ware
        Brazing alloys and solders
        Other
       38
    
       26
    
       17
        7
       12
       39
    
       25
    
       15
        8
       13
    U.S.  Bureau of Mines, 1980.
                                      9-61
    

    -------
                      Table 9-35.   PRICE HISTORY:   SILVER'
    
    Year
    1955
    1956
    1957
    1958
    1959
    1960
    1961
    1962
    1963
    1964
    1965
    1966
    1967
    1968
    1969
    1970
    1971
    1972
    1973
    1974
    1975
    1976
    1977
    1978
    Oct.b
    1979
    Actual
    $/kg
    28.94
    28.94
    28.94
    28.94
    28.94
    28.94
    29.58
    34.72
    40.83
    41.47
    41.47
    41.47
    49,83
    68.80
    57.55
    56.91
    49.51
    54.01
    82.31
    151.43
    142.11
    139.86
    148.54
    171.04
    
    539.67
    prices
    $/troy oz
    0.90
    0.90
    0.90
    0.90
    0.90
    0.90
    0.92
    1.08
    1.27
    1.29
    1.29
    1.29
    1.55
    2.14
    1.79
    1.77
    1.54
    1.68
    2.56
    4.71
    4.42
    4.35
    4.62
    5.32
    
    16.78
    Based
    1977
    $/kg
    67.20
    64.94
    63.02
    62.05
    60.44
    59.48
    60.44
    69.45
    80.70
    80.70
    78.77
    76.20
    89.06
    117.67
    93.88
    88.09
    72.98
    76.20
    109.96
    184. 55
    157.86
    147.57
    148. 54
    — —
    
    
    on constant
    dollars
    $/troy oz
    2.09
    2.02
    1.96
    1.93
    1.88
    1.85
    1.88
    2.16
    2.51
    2.51
    2.45
    2.37
    2.77
    3.66
    2.92
    2.74
    2.27
    2.37
    3.42
    5.74
    4.91
    4.59
    4.62
    ~ •"
    
    
    ^Average annual  price of silver metal from Drake (1978).
    3Average price for October from Engineering and Mining Journal (1979),
                                       9-62
    

    -------
                     Table  9-36.   PRODUCTION  PROFILE:   SILVER"
         Parameter
                         Year
                                      1974
                 1975
          1976
          1977
          1978
    Production, 1,000 kg  (1,000
      as metal
      Mine
      Refinery:  New
                 Secondary (old
                   scrap)
    Ibs)
                           b
    Imports for consumption
      1000 kg (1,000 Ibs)
      as metal
    Exports0, 1000 kg (1,000
      Ibs) as metal
    
    Employment:   mine and mill
    
    Net import reliance0 as a
      percent of apparent con-
      sumption
        1,086   1,122   1,102
       (2,394) (2,474) (2,429)
    
        2,035   2,038   1,749
       (4,486) (4,493) (3,856)
        1,739   1,594   1,614
       (3,834) (3,514) (3,558)
    
        3,035   2,138   2,337
       (6,691) (4,713) (5,152)
           591   1,048     469
       (1,303) (2,310) (1,034)
                 1,228   1,228
                (2,707) (2,707)
    
                 1,446   1,696
                (3,188) (3,739)
                 1,540   1,156
                (3,395) (2,549)
    
                 2,543   2,593
                (5,606) (5,717)
                    720     768
                (1,587) (1,693)
        1,350    1,250   1,450   1,450   1,500
           44
    12
    45
    31
    48
    aU.S.  Bureau of Mines, 1980.
     Excludes coinage.
    °Net import reliance = imports-exports+adjustments for Government and
    industry stock changes.
                                       9-63
    

    -------
                  Table 9-37.   INDUSTRY CHARACTERISTICS:   SILVER
    Number of leading companies
    
    Number of active operations
    Percent of capacity controlled by leading
      companies
    
    Value of processing plant output
      (as metal)
    
    Major processing states
    
    Ratio of ore to product
    11 (1 temporarily
      inactive, 1 under
      construction)
    85
    
    
    $103.1 million
    
    Idaho, Colorado
    
    Range:  1,150 - 30,000
    Typical:  8,400
                                        9-64
    

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    -------
    9.1.8  Titanium
         Most titanium  is consumed as titanium dioxide pigment (see
    Table 9-39).  The pigment has a high refractive  index and is used in
    surface coatings, paints, paper coatings, photographic papers, paper
    boxes, and plastics to add whiteness and opacity.  Titanium metal is
    used mainly in aircraft and guided missile assemblies, spacecraft, and
    aircraft turbine engines.  It is also used by the chemical and
    electrochemical processing industry, and in steel and other alloys.
    Table 9-40 profiles the production statistics of this industry.
         Possible substitutes for titanium pigments  include zinc oxide,
    talc, clay, silica, and alumina.  However, they cost more and do not
    perform as well.  High strength, low alloy steels, aluminum or other
    metals can replace titanium metal in some structural applications, but
    they usually do not perform as well and require redesigning of products
    and manufacturing methods.  Nickel steels are somewhat competitive in
    structural applications. When titianium metal is chosen for its resistance
    to corrosion, stainless steel, Hastelloy, 90 copper-10 nickel, and
    certain nonmetals may be substituted.
         The mineral sources of titanium are rutile and ilmenite.
    Concentrates of these minerals are made at relatively few operations in
    the world.  These deposits (rutile and ilmenite) may be either sand or
    rock.  Both rutile and ilmenite occur together in sand deposits, but
    ilmenite is the main constituent of rock deposits.   Large deposits of
    rutile are found on Australia's east and west coast, and the United
    States demand for rutile is met largely by imports.   Domestic sand
    deposits contain approximately 1.0 to 2.0 percent titanium as titanium
    dioxide.
         Processing of titanium ores is controlled by the three major
    companies shown in Table 9-41.   Titanium processors are listed in
    Table 9-42.   Most United States processing of titanium ores is a part of
    an integrated operation.   Over 95 percent of the world's natural rutile
    production is from Australia.
         Table 9-43 includes the price history for titanium, both as rutile
    pigment and sponge metal.   Both forms were characterized by current
    dollar price stability until  1974 when prices began to rise.   In constant
    dollars,  prices were falling through 1974.
    
                                     9-67
    

    -------
         Demand for titanium is expected to increase by about 4.3 percent
    per year through 1985.  A 270 Mg per hour expansion to an existing plant
    and a 540 Mg per hour new plant are projected by 1985.  These plants are
    assumed to process sand-type ore with a titanium content of 1.5 percent
    as titanium dioxide and 0.9 percent zirconium.
                                      9-68
    

    -------
                      Table 9-39.  PRODUCT USES:  TITANIUM0
        Product uses
      1978
    (percent)
        Paints
        Paper
        Plastic
        Sponge metal
        Other uses
       50
       21
       12
        2
       15
    Lynd, 1978 and U.S.  Bureau of Mines, 1980.
                                      9-69
    

    -------
                    Table 9-40.   PRODUCTION PROFILE:   TITANIUM0
         Parameters
                                                      Year
                                     1975
              1976
    1977
                                                             1978
      1979
    Production (Mg as metal)
    
    Imports for consumption, Mg
      (ton) as sponge metal
    
    Exports (mainly scrap), Mg
      (ton)
    
    Price:  sponge, per pound
      year end
    
    Stock:  Sponge, industry,
      year end
    
    Net import reliance0 as a
      percent of  apparent  con-
      sumption
     3,800   1,613   2,165   1,339   2,177
     (4,190)  (1,778) (2,387) (1,476) (2,400)
    
     5,647   6,538   4,031   7,065   6,984
     (6,226)  (7,209) (4,444) (7,789) (7,700)
    
     $2.70     $2.70    $2.98   $3.28   $3.98
      5,669   3,617    3,546    2,642    1,300
    Titanium Dioxide:
    Production
    
    Imports  for consumption,
       Mg (ton)
    
    Exports, Mg (ton)
     Employment
    
     Net import reliance  as a
       percent of apparent
       consumption
    603,429   712,940   687,103   720,223  724,000
    
     23,562    62,270   104,373   107,000  105,450
    (25[918)  (68,497) (114,810) (117,708)(116,000)
    
     14,337    18,912    14,817    34,296   44,444
    (15,807)  (20,850)  (16,336)  (37,812) (49,000)
      5,800
    
      Net
      exporter
                                               4,900
        4,900
    
           12
    4,200
    
       12
    4,800
    
       12
     aU.S. Bureau of Mines, 1980.                  .
     Withheld to avoid disclosing company proprietary information.;
     cNet import reliance = imports-exports+adjustments for Government and
     industry stock.                               ..
                                        9-70
    

    -------
                 Table 9-41.   INDUSTRY CHARACTERISTICS:   TITANIUM
    Number of leading companies (titanium
      and zirconium)
    Number of active operations (titanium
      and zirconium)
    Percent capacity controlled by leading
      companies
    Value of processing plant output
      (as ilmenite/zircon concentrate)
    Major processing states
    Ratio of ore to product
    5 (2 inactive)
    
    98
    
    $70.5 million
    Florida, New Jersey
    75 to 100 (as Ti02 in
      sand-type ores)
                                       9-71
    

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    9-72
    

    -------
                      Table 9-43.  PRICE HISTORY:  TITANIUM'
    
    Based on constant
    Year
    
    
    
    1954
    1955
    1956
    1957
    1958
    1959
    1960
    1961
    1962
    1963
    1964
    1965
    1966
    1967
    1968
    1969
    1970
    1971
    1972
    1973
    1974
    1975
    1976
    1977
    1978
    1979
    1980
    Actual
    Ruti 1 e
    pigment
    $/lb
    0.41
    0.41
    0.44
    0.46
    0.46
    0.46
    0.46
    0.46
    0.46
    0.46
    0.46
    0.46
    0.46
    0.46
    0.48
    0.48
    0.45
    0.45
    0.45
    0.50
    0.72
    0.73
    0.78
    0.81
    0.85
    1.02
    1.15
    price
    Sponge
    metal
    $/lb
    4.80
    3.90
    3.20
    2.50
    2.05
    1.66
    1.60
    1.60
    1.60
    1.60
    1.32
    1.32
    1.32
    1.32
    1.32
    1.32
    1.32
    1.32
    1.32
    1.42
    2.25
    2.70
    2.70
    2.98
    3.28
    3.98
    7.02
    1976
    Ruti 1 e
    pigment
    $/lb
    0.92
    0.90
    0.94
    0.95
    0.93
    0.91
    0.90
    0.89
    0.87
    0.86
    0.85
    0.83
    0.80
    0.78
    0.78
    0.74
    0.66
    0.63V
    0.60
    0.63
    0.83
    0.77
    0.78
    0.77
    —
    --
    — —
    dollars
    Sponge
    metal
    $/lb
    10.76
    8.57
    ' 6.80
    5.14
    4.16
    3.29
    3.12
    3.09
    3.04
    2.99
    2.43
    2.38
    2.30
    2.24
    2.14
    2.04
    1.94
    1.84
    1.77 '
    1.80
    2.60
    2.84
    2.70
    2.82
    —
    —
    ——
     Year-end price as rutite pigment (Ti content) and sponge metal from
    Lynd (1978).
                                       9-73
    

    -------
    9.1.9  Tungsten
         Tungsten's unique high temperature properties make it suitable  for
    many industrial uses.  As a carbide, its hardness makes it useful  as a
    cutting edge or facing material in industrial  equipment.   As an alloy
    constituent, tungsten is used in steels that require resistance to wear,
    abrasiveness, shock, and corrosion or that need strength at high
    temperatures.  Mill products made from pure tungsten metal powder are
    used in the electrical and electronic industries, furnaces, aircraft,
    and in the aerospace industry.  Tungsten is also used in various
    chemicals and compounds.  Product uses are presented in Table 9-44.
         The increasing price of tungsten, as shown in Table 9-45, has
    resulted in the expanded use of secondary scrap.  Tungsten demand in the
    United States is linked to major end uses that depend on wear-resisting
    materials, and these uses constitute about 72 percent of tungsten
    consumption.  Alumina may substitute for tungsten in some instances
    where an abrasive, wear-resistant material is required.  However, in
    most cases substitution brings impaired performance.   An early break-
    through in ceramic technology, in applications  involving high
    temperatures and oxidation resistance could affect demand for tungsten.
    However, this technology has  not been commercially developed.
         Most tungsten ore  has come from the Bishop mine of the Union Carbide
    Company, which is the leading company noted on  Table 9-46, and the
    Climax mine  of AMAX,  Incorporated (listed  in Table 9-33).  Five tungsten
    ore processing plants are  listed  in Table  9-47.   Because of tungsten's
    partial association  with molybdenum,  about 25 percent  of future domestic
    production  may be  determined  by the level  of molybdenum mining operations.
    Although  United  States  tungsten reserves are relatively small, research
    on tungsten recovery and utilization  continues.!  Anticipated  improvements
    in tungsten processing  would  allow  more effective development of  high
    volume,  low-grade  deposits.   Domestic tungsten  deposits are  usually less
    than  1 percent tungsten and  are typically  in the range of  0.4 to
    0.5  percent.   For  the near future the United States  will  continue to
    depend heavily on  imports  as  shown  in Table  9-48.
          Demand for  tungsten is  expected  to increase by  approximately
    5 percent per year through 1985.  Tungsten ore  processing capacity  is
                                      9-74
    

    -------
    projected to increase as a result of a new 23 Mg per hour plant processing
    ore containing 0.5 percent tungsten.   These growth projections may be
    disrupted if the General Services Administration continues its sales of
    large quantities of ferrotungsten from the government's strategic
    materials stockpile.
                                     9-75
    

    -------
    Table 9-44.  PRODUCT USES:   TUNGSTElf
    
    Product uses
    Metal working and construction
    machinery
    Transportation
    Lamps and Lighting
    Electrical
    Other
    1978
    (percent)
    75
    11
    7
    4
    3
    1979
    (percent)
    77
    10
    6
    4
    3
    aU.S. Bureau of Mines, 1980.
                     9-76
    

    -------
                      Table 9-45.  PRICE HISTORY:  TUNGSTEN1
    Year
     Actual prices
    $7kg       !7Tb
    Based on constant
      1976 dollars
                                                        $7kg
                  $7lb
    1956
    1957
    1958
    1959
    1960
    1961
    1962
    1963
    1964
    1965
    1966
    1967
    1968
    1969
    1970
    1971
    1972
    1973
    1974
    1975
    1976
    1977
    Oct.
    1979
    8.05
    3.44
    2.45
    2.87
    3.09
    2.98
    3.20
    2.95
    2.82
    3.79
    4.63
    4.10
    4.94
    5.22
    5.62
    6.53
    5.64
    5.97
    10.52
    11.55
    14.42
    21.54
    
    17.97
    3.65
    1.56
    1.11
    1.30
    1.40
    1.35
    1.45
    1.34
    1.28
    1.72
    2.10
    1.86
    2.24
    2.37
    2.55
    2.96
    2.56
    2.71
    4.77
    5.24
    6.54
    9.77
    
    8.15
    17.13
    7.08
    4.96
    5.69
    6.02
    5.75
    6.06
    5.51
    5.20
    6.83
    8.07
    6.94
    8.00
    8.07
    8.25
    9.10
    7.56
    7.56
    12.13
    12.17
    14.42
    20.39
    
    --
    7.77
    3.21
    2.25
    2.58
    2.73
    2.61
    2.75
    2.50
    2.36
    3.10
    3.66
    3.15
    3.63
    3.66
    3.74
    4.13
    3.43
    3.43
    5.50
    5.52
    6.54
    9.25
    
    —
     Average annual  price per pound of tungsten contained in concentrate
    (65% W03).
    
     Average price for October from Engineering and Mining Journal  (1979).
                                       9-77
    

    -------
                 Table 9-46.   INDUSTRY CHARACTERISTICS:   TUNGSTEN
    Number of leading companies
    
    Number of active operations
    
    
    Percent capacity controlled by
      leading companies
    
    Value of concentrate production
      (as 65 percent W03 concentrate)
    
    Major processing states
    
    Ratio of ore to product
    4 (1 temporarily
      inactive)
    71
    
    
    $45 thousand
    
    California, Nevada
    
    Range:  150 - 250
    Typical:  200
                                        9-78
    

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    9-79
    

    -------
                    Table 9-48.   PRODUCTION PROFILE:   TUNGSTEN0
         Parameters
                                     1974
                                                     Year
             1975    1976
                    1977
                   1978
    Production; mine shipments,
      1,000 Mg (1,000 Tons)
      as metal
    
    Imports for consumption; as
      concentrate, 1,000 Mg
      (1,000 Tons)
    
    Exports; as concentrate,
      1,000 Mg (1,000 Tons)
    
    Employment:  mine and mill
    
    Net import reliance  as a
      percent of apparent con-
        sumption
     3.55    2.49    2.66    2.73    3.14
    (3.91)  (2.74)  (2.93)  (3.01)  (3.46)
     5.03
    (5.54)
     0.54
    (0.60)
    
      540
       57
     2.98   2.40    3.14    4.15
    (3.28) (2.64)  (3.46)  (4.57)
     0.60   0.78
    (0.66) (0.86)
      525
       46
    540
     53
           0.58    0.84
          (0.64)  (0.93)
    945
     52
    875
     56
    aU.S. Bureau of Mines, 1980.
    bNet import reliance = imports-exports+adjustments for Government and
    industry stocks..
                                        9-80
    

    -------
    9.1.10  Uranium
         In its natural state, uranium contains about 0.7 percent of isotope
    U-235, the critical isotope in the generation of nuclear fision processes.
    Most uranium is purchased by utilities to fuel nuclear reactors as
    indicated in Table 9-49.  Depleted uranium (a byproduct of the enrichment
    of natural uranium) is used primarily in ordnance, as well as for
    containers of spent nuclear reactor residues and other radiation shields
    for counterweights and ballast for aircraft and ships, and in research.
    The supply of this byproduct greatly exceeds demand.
         There are no substitutes for uranium in the production of nuclear
    energy, although thorium and plutonium are supplements.  Lead, tungsten,
    and other metals can replace uranium in nonnuclear applications.
         Industry characteristics are presented in Table 9-50.  The major
    oil companies, such as Kerr-McGee, Exxon, Gulf, and Getty, dominate all
    phases of the domestic uranium industry.  Union Carbide, United Nuclear,
    and Lucky McMines (an independent subsidiary of General Electric) are
    other large processors of uranium.  Thirty-two uranium processing plants
    are listed in Table 9-51.
         During the sixties and seventies, many uranium mines and mills
    operated with ore that contained approximately 0.2 percent uranium.
    Because the richer deposits have been exhausted, the ore grade in new
    mines has fallen to 0.10 to 0.15 percent uranium.  Ore grades for new
    mining sites are projected at 0.13 percent uranium.
         Demand for uranium has been projected to increase by 15 percent per
    year through 1985.  The controversy surrounding the nuclear industry
    following the Three Mile Island incident and the accelerating cost of
    nuclear construction coupled with the decreasing growth in demand for
    electrical power may reduce the growth rate in the uranium industry.   In
    addition, the price of uranium has declined as shown in Table 9-52.
    Growth in capacity in the uranium industry is expected to include two
    23 Mg per hour plants and three 68 Mg per hour plants by 1985.
                                     9-81
    

    -------
                       Table 9-49.   PRODUCT USES:  URANIUMC
         Product uses
      1978
    (percent)
         Fuel
    
         Nonnuclear
       98
    
        2
    aU.S. Bureau of Mines, 1980.
                                        9-82
    

    -------
                  Table 9-50. INDUSTRY CHARACTERISTICS:  URANIUM
    Number of leading companies
    
    Number of active operations
    Percent of capacity controlled by leading
      companies
    
    Value of processing plant output
      (as yellowcake U30g)
    
    Major processing states
    Ratio of ore to product
     10
    
     31 (1 temporarily
       inactive)
     74
     $1608.7  million
    
     New Mexico, Wyoming,
       Colorado
    
    .Range:   500 -  1,000
             850 (future growth)
                                       9-83
    

    -------
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                Table  9-52.   PRODUCTION  PROFILE  AND  PRICE HISTORY:
                                    URANIUM3'D
    
    Parameters
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    Uranium content Mg (tons)
    Imports, concentrate, Mg
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    Employment (reduction plants)
    Average annual price (U30g)
    Dollars per kg
    Dollars per pound
    
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    Year
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    (12, 410)(12, 296)(13,997)
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    11.45 23.68
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    3,629
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    66.12
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    aU.S. Bureau of Mines, 1980.
    American Metal Markets, 1978.
    c$ per pound U308 as of October 31, 1980 from the Engineering and
    Mining Journal (1979).
     For nonenergy applications.
                                        9-88
    

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               Table  9-52.   PRODUCTION  PROFILE  AND  PRICE  HISTORY:
                                    URANIUMa'D
    
    Parameters
    Production
    Ore, 1,000 Mg (1,000 tons)
    Uranium content Mg (tons)
    Imports, concentrate, Mg
    (tons) as metal
    Employment (reduction plants)
    Average annual price (UgOg)
    Dollars per kg
    Dollars per pound
    
    1974
    6,456
    (7,115)
    
    1975
    6,681
    (7,362)
    Year
    1976
    8,344
    (9,195)
    11,261 11,158 12,701
    (12,410)(12,296)(13f997)
    1,665
    (1,835)
    —
    25.24
    11.45
    1,112
    (1,225)
    100
    52.20
    23.68
    5,023
    (5,535)
    200
    87.52
    39.70
    
    	 — 	 FT
    1977 Oct. 1979~
    NA
    13,608
    (14,996)
    3,629
    (3,999)
    300
    93.03
    42.20
    NA
    NA
    NA
    NA
    NA
    NA
    66.12
    30.00
    aU.S. Bureau of Mines, 1980.
    
    American Metal Markets, 1978.
    
    c$ per pound U308 as of October 31, 1980 from the Engineering and
    Mining Journal (1979).
    
     For nonenergy applications.
                                        9-88
    

    -------
    9.1.11  Zinc
         Zinc is extremely versatile and has a number of uses as an alloy
    ingredient, a protective coating, and a chemical compound.  Table 9-53
    summarizes product uses of zinc.  Most zinc goes to the construction
    industry where it is used in the galvanization of many materials.  The
    transportation industry also uses zinc for galvanization, in die castings
    for automotive components, and in rubber for tires.  Zinc is used in
    electrical equipment, office equipment and machinery, in sensitizing
    photocopying paper, as well as in a number of other applications.
         Aluminum, magnesium, and plastics replace zinc in diecasting where
    weight limitations or surface finishes are important factors.  The price
    of substitutes and zinc's superior durability affect the degree to which
    these substitutions are made.  In many cases, the automobile industry
    has moved to lighter weight materials.   Aluminum, magnesium, titanium
    oxides, and zirconium compounds are competitive in the chemical and
    pigment applications of zinc.
         Zinc prices (covered in Table 9-54) and demand are correlated with
    general economic activity due to zinc's use in the construction and
    transportation industries.  The producers of zinc also face competition
    from imports as indicated on Table 9-55.  Lead and zinc are often
    processed in the same plant.   Forty-three of the plants listed in
    Table 9-28 process zinc either alone or as a coproduct with lead.
    Table 9-56 lists additional industry characteristics.   When mined in
    conjunction with lead, the concentration of zinc typically averages
    1 percent.
         Demand for zinc is expected to increase at about 2 percent per year
    through 1985.   The three prospective new zinc processing plants were
    covered under the section on lead (Section 9.1.5).   These facilities are
    expected to process both lead and zinc with a zinc ore grade of 1 percent.
                                     9-89
    

    -------
                       Table  9-53.   PRODUCT  USES:  ZINCC
        Product uses
      1978
    (percent)
      1979
    (percent)
        Construction materials
        Transportation equipment
        Electrical equipment
        Machinery and chemicals
        Other
       41
       27
       10
        8
       14
       40
       26
       12
       10
       12
    U.S. Bureau of Mines, 1980.
                                       9-90
    

    -------
                        Table 9-54.  PRICE HISTORY:  ZINCC
    Year
     Actual prices
    
    -------
                     Table 9-55.  PRODUCTION PROFILE:  ZINCC
    
    Parameters
    Production 1,000 Mg (1,000
    as metal
    Mi ne
    l l l l it-
    Primary slab zinc
    
    1974
    tons)
    
    453
    (499)
    504
    (555)
    Secondary redistilled slab 71
    zinc . (78)
    Imports for consumption, 1
    (1,000 tons) as metal
    Ore and concentrates
    Slab zinc
    Exports: Slab zinc, 1,000
    (1,000 tons) as metal
    Employment:
    Mine and mill0
    Smelter
    Net import reliance as a
    percent of apparent con-
    sumption
    ,000 Mg
    
    121
    (133)
    493
    (543)
    Mg 17
    (19)
    
    6,700
    4,500
    
    59
    
    1975
    
    
    426
    (469)
    397
    (437)
    53
    (58)
    
    
    389
    (429)
    340
    (375)
    6
    (7)
    
    6,700
    4,100
    
    61
    Year
    1976
    
    
    440
    (485)
    453
    (499)
    62
    (68)
    
    
    141
    (155)
    631
    (695)
    3
    (3)
    ".:
    6,700
    .4,100
    
    58
    
    1977
    
    
    408
    (450)
    408
    (450)
    46
    (51)
    
    
    109
    (120)
    504
    (555)
    b
    
    6,600
    4,100
    
    57
    
    1978
    
    
    303
    (334)
    407
    (449)
    35
    (39)
    
    
    106
    (117)
    622
    (685)
    1
    (1)
    
    5,700
    4,100
    
    66
    aU.S. Bureau of Mines, 1980.
    bl_ess than one-half unit.
    clncludes all zinc and/or lead-zinc producing units.
    dNet import reliance = imports-exports+adjustments for Government and
    industry stock changes.
                                       9-92
    

    -------
                   Table 9-56.   INDUSTRY CHARACTERISTICS:   ZINC
    Number of leading companies (lead/zinc)
    
    Number of active operations (lead/zinc)
    
    
    Percent of capacity controlled by
      leading companies (as 95 percent
      ZnS + PbS concentrate)
    
    Major processing states
    
    
    Ratio of ore to product
    8
    
    46 (11 temporarily
      inactive)
       .9 million
    Missouri, Idaho,
      New Jersey
    
    Range:  10 •- 100
    Average:  25
    New lead/zinc
      plants:  100
                                        9-93
    

    -------
    9.1.12  Zirconium
         Zirconium, covered by Tables 9-57 through 9-60, is consumed in two
    basic forms:  zircon (zirconium silicate) which represents over 90 percent
    of production tonnage, and zirconium metal.  As indicated in Table 9-59,
    zircon is used in foundry sands, refractories, abrasives, ceramics, and
    as a source of zirconium metal.  Zirconium metal is used in nuclear
    reactors, corrosion resistant industrial equipment, flash bulbs, and as
    a refractory alloy.  Commercial nuclear generating plants consume over
    90 percent of nonmilitary zirconium metal production.  Zircon may be
    replaced in certain foundry applications by chromite and some aluminum
    silicate minerals.  There are no ready substitutes for zirconium in its
    nuclear uses.
         Plants that process zirconium and titanium as their main product
    are listed in Table 9-42.  Demand for zircon is expected to increase at
    an annual rate of around 3 percent through 1985 (United States Bureau of
    Mines, 1980).  New demand will be met from the production of zirconium
    as a coproduct of titanium from sand-type ores (see Section 9.1.8).
    Based on the ore grades of existing plants, an ore grade of 0.9 percent
    (as zircon) was assumed for new plants.
    9.1.13  Strategic Stockpile
         Many of the metals or metallic minerals under consideration for
    this NSPS are stockpiled in various forms by the United States government
    for strategic reasons.  Table 9-61 lists the metals and the metallic
    form stockpiled.  Actual quantities stockpiled and the respective  stock-
    pile goals; are also given.  The stockpiling efforts of the United  States
    government have sometimes been characterized as erratic and stockpiling
    activities do not  necessarily follow articulated policies.  For the year
    1979, the only two metals subject to government sales were tungsten and
    gold.  Tungsten sales  amounted to 4,250,000 pounds of ores and
    concentrates.
                                      9-94
    

    -------
                   Table 9-57.   PRODUCTION PROFILE:   ZIRCONIUM1
         Parameters
         	Year	
       1974    1975    1976    WTT   1978"
    Production Mg (tons)
      Zircon
      Zirconium metal
    Imports Mg (tons)
      Zircon
    
      Zirconium metal
    
    Exports Mg (tons)
      Zircon
      Zirconium, alloys, and
        scrap
    Employment
           b
           b
    b
    b
    b
    b
    b
    b
    b
    b
     56,703   36,474  58,644  59,153  82,730
    (62,487) (40,194)(64,626)(65,187)(91,168)
        332      738     452     580     900
       (366)    (813)   (498)   (639)    (992)
     19,493   17,024   8,553  13,029   6,974
    (21,481) (18,760) (9S429)(14,358) (7,685)
        748    1,202   1,045
       (824)  (1,325) (1,152)
                  891     936
                 (982) (1,031)
    Mine and mill
    Metal plant
    Net import reliance0 as a
    percent of apparent con-
    sumption
    500
    900
    b
    550
    850
    b
    550
    800
    b
    550
    800
    b
    500
    750
    b
    aU.S. Bureau of Mines, 1980.
    Withheld.
    cNet import reliance = imports-exports+adjustments for Government and
    industry stock changes.
                                       9-95
    

    -------
                     Table 9-58.  PRICE HISTORY:  ZIRCONIUM0
    
    Year
    1974
    1975
    1976
    1977
    1978
    1979
    $/Mg
    331
    232
    . 165
    165
    201
    165
    $/Short ton
    . 300
    210
    150
    150
    183
    150
    Average annual price of Zirconium concentrate (65 percent ZrO^) from
    Engineering and Mining Journal.
                                      9-96
    

    -------
                      Table 9-59.   PRODUCT USES:   ZIRCONIUM1
         Product uses
      1978
    (percent)
      1979
    (percent)
         Foundry sands
         Refractories
         Ceramics
         Abrasives
         Miscellaneous  uses,  including
           nuclear
       42
       30
       12
        4
    
       12
       42
       30
       12
        4
    
       12
    *U.S.  Bureau of Mines,  1980.
                                       9-97
    

    -------
                 Table 9-60.   INDUSTRY CHARACTERISTICS:   ZIRCONIUM
    Number of leading companies
      (titanium and zirconium)
    
    Number of active operations
    Precent capacity controlled by
      leading companies
    
    Value of processing plant output
      (as ilmenite/zircon concentrate)
    
    Major processing states
    
    Ratio of ore to product (as zircon)
    5 (1 temporarily
      inactive)
    98
    
    
    70.5
    
    Florida, New Jersey
    
    100
                                        9-98
    

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    9.1.14  REFERENCES FOR SECTION 9.1
    
    American Metal Market.  1978.  |letal Statistics.  Fairchild
         Publications. New York. ^fT. 253-254v
    
    Baumgardner, L.  United States Bureau of Mines.   1981.  Telephone
         conversation with M. Buckwalter, TRW.  February  11.   Discussion  of
         ore grades for bauxite processing plants.
    
    Butterman, W. C. 1978.  Gold:  Mineral Commodity  Profile.  U.S.  Bureau
         of Mines.  Washington, D. C. 17pp.
    
    Carter, R. A.  1978.  Nations Newest Silver Mine  Uses Open-Pit  Methods.
         Mining Engineering,  p. 41-44.
    
    Cammarota, V. A.  1978.  Zinc:  Mineral Commodity Profile.   U.S. Bureau
         of Mines.  Washington, D. C.  25pp.
    
    Drake, H.  J.  1978.  Silver:  Mineral Commodity Profile.   U.S.  Bureau of
         Mines.  Washington, D. C.  14pp.
    
    Engineering and Mining Journal.  1979.  Engineering and Mining  Journal
         Markets.  180(5):  p. 19-25.
    
    Engineering and Mining Journal.  1980.  1980  Survey of Mine  and Plant
         Expansion.  181(1):  p. 76-90.
    
    Etheridge, D. A.  1980.  Gold.  Engineering and Mining Journal.  181(3):
         p. 120-23.
    
    Klinger, F. L.  1978.  Iron Ore:  Mineral Commodity Profile.  U.S.
         Bureau of Mines.  Washington, D. C.  27pp.
    
    Kornhauser, B. A. and Philip T. S.  1978.  Tungsten:  Mineral Commodity
         Profile.  U.S. Bureau of Mines.  Washington, D.  C. 22pp.
    
    Kummer, J. T.  1979.  Molybdenum:  Mineral Commodity  Profile.   U.S.
         Bureau of Mines.  Washington, D. C.  23pp.
    
    Lynd, L. F.  1978.  Titanium:  Mineral Commodity  Profile.  U.S.  Bureau
         of Mines.  Washington, D. C.  19pp.
    
    Mining Information Services.  1979.  International Directory of Mining
         and Mineral Processing Operations.  Engineering  and  Mining Journal
         (McGraw Hill).  New York.  p. 11-242.
    
    Ryan, J. P. and J. M. Hague.  1977.  Lead:  Mineral Commodity Profile.
         U.S.  Bureau of Mines.  23pp.
    
    Schroeder, H. J.  1979.  Copper:  Mineral Commodity Profile.  U.S.
         Bureau of Mines.  Washington, D. C.  20pp.
                                     9-101
    

    -------
    Stamper, J. W. arid H.' F. Kurtz., 1978.  Aluminum:  Mineral Commodity
         Profile.  U.S. Bureau of Mines.  Washington, D. C.  29pp.
    Stephenson, P.-  U.S. Bureau of  Mines.  1981.  Telephone conversation
         with M. Alexander, 'TRW.  February 11.  Discussion of  start-up  dates
         and mill-capacity  for bauxite  processing plants.
    United States Bureau of Mines.   1980.  Mineral  Commodity Summaries.
    Veith, D.  Minnesota Bureau of  Mines.  1980.  Telephone conversation
         with  E. Monnig, TRW.  July 23.   Discussion of  nickel  mining in
         Minnesota.
                                      9-102
    

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     9.2  ECONOMIC IMPACT ASSESSMENT
     9.2.1  Introduction and Summary
          9-2.1.1  Introduction.   This section  assesses  the economic  impact
     of the regulatory alternatives on the  metallic mineral processing industries.
     Economic profile information on the industries presented in Section 9.1 is a
     principal  input to this assessment.  For the purpose of economic analysis
     the 12 metals are divided  into ten industries.   In  the economic  analysis lead
     and zinc are treated as coproductscof  a single industry, as are titanium and
     zirconium.   Various financial  analysis techniques are applied to the model
     plants to  determine potential  impacts on control affordability and control
     capital  availability.   These findings are  assessed, based on the industry
     profile, to  determine the  industry-wide impacts that will be presented in
     Section  9.3.
          As  noted in  previous  chapters the facilities of interest, located at the
     crude ore milling  stage  of the  production process, are:  crushers,  screens,
     ore bins, hammer mills,  dryers, product transfer points and product loadout
     facilities.   Model  plants for some of the metals contain all of the facili-
     ties  of  interest,  but not every model plant contains every facility of
     interest.
          9.2.1.2  Summary.   Table 9-62 lists the percentage price increases,  the
     percentage capital cost  increases, and the affordability conclusions,  using
     the most costly regulatory alternative for all  industries and model  plant
     sizes.  The most costly regulatory alternative  for each model  plant  refers to
     the regulatory alternative that has the highest net annualized cost, which is
     alternative 3b.
         A screening analysis shows that none  of the  ten industries is  likely to
     experience a significant impact for any model plant size  when the most
    costly regulatory alternative is added.  Each of  the ten  products would
    require a sales price increase, usually at  the  refined  metal  stage of  proces-
    sing, of two percent or  less  when the most  costly regulatory alternative  is
    added.
         Because the most costly  regulatory alternative  (3b)  is  likely to  be
    affordable,  the less costly alternatives (2 and 3a)  are also  affordable
    and therefore a separate analysis  of  these  alternatives is not  provided.
                                         9-103
    

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        Table 9-62.  SUMMARY OF PRICE INCREASE
    FOR THE MOST STRINGENT REGULATORY ALTERNATIVE
    Cents Percentage
    Plant Size Per Pound Price
    Metal (TPH)
    1. Aluminum (150)
    (300)
    2. Copper (150)
    (600)
    3. Gold (75)
    (150)
    4. Iron Ore (1200)
    '(2400)
    5. Lead/Zinc*** (300)
    (600)
    6. Molybdenum (300)
    (1200)
    7. Silver (50)
    (150)
    8. Titanium/ (300)
    Zirconium (600)
    (sand)
    9. Tungsten (25)
    10. Uranium (25)
    (75)
    Ins. = insignificant (<
    Increase Increase
    0.02
    0.02
    1.6
    0.8
    84. (troy oz)*
    52. (troy oz)
    0.16 (LTU)**
    0.18 (LTU)
    . 0.1
    0.1
    1.1
    0.6
    7. (troy oz)
    3. (troy oz)
    0.1
    0.1
    ••/
    3.6 ^
    8.8 ''
    3.6
    .1 percent)
    Ins.
    Ins.
    1.7
    0.8
    0.2
    0.1
    0.2
    0.3
    0.2
    0.2
    0.1
    0.1
    0.5
    0.2
    0.8
    0.8
    
    0.5 ,
    0.2
    0.1
    
    Capital
    Control
    Percent Affordability
    Increase
    Ins.
    Ins.
    0.2
    0.2
    0.2
    0.2
    0.1
    0.1
    0.2
    0.2
    0.2
    0.2
    0.4
    0.2
    0.9
    ; !-2
    
    1.0 ;
    ' 0.8
    0.3
    
    Conclusion
    affordable
    affordable
    affordable
    affordable
    affordable
    affordable
    affordable
    affordable
    affordable
    affordable
    affordable
    affordable
    affordable
    affordable
    affordable
    affordable
    
    affordable
    .affordable
    affordable
    
    *14.5 Troy Ounces = 1 pound avoirdupois
    **1 Long Ton Unit (LTU)
    ***Note the discussion in
    = 22.4 pounds
    Section 8.1 on the possible
    effects of the
    
    .NAAQS for lead on the calculation of the control costs for lead/zinc.
    processing plants.
    
    — .
    9-104
    
    
    
    ^^__^1_
    
    I^H^^H
    

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     9.2.2  Methodology
          This section describes  the methodology used to  assess the economic
     impact of the regulatory alternatives  on  the ten industries that include 19
     model plants.  The principal  economic  impact which is assessed is the effect
     of incremental  control  costs on the  profitability of new grassroots plants,
     or expansions of  existing plants.  Expansions of existing plants are repre-
     sented by the smaller model  plant  sizes and therefore a separate analysis for
     expansions is not necessary.
          Since each state implementation plan (SIP) contains particulate emission
     control  standards, any  new plant would have to meet  SIP standards even in
     the absence of  a  NSPS.   Incremental  control  costs are the control costs
     above those baseline costs required  to meet the various SIP standards.
          In  the analysis which follows,  each  model plant is evaluated as if it
     stands alone, that is,  the firm is not associated with any other business
     activity nor is it associated with any larger parent company.  This assump-
     tion has the effect of  isolating the control  cost without any assistance from
     other business  activities or firms.  This is a conservative assumption because
     many of  the companies in  the metallic  mineral processing industries are large
     corporations with substantial  management, financial, and other resources, any
     or all of which could be  used to aid other product lines or subsidiaries.
     For example, a  parent corporation could lend money to a subsidiary, or a
     parent corporation could  guarantee repayment of a subsidiary's loan.
          This analysis assumes that a plant is profitable in the absence of a
     NSPS.  Therefore,  the focus  of this  analysis is on incremental costs to
     determine if a  plant which would o'therwise be profitable is now rendered
     unprofitable as a result  of  the incremental  control  costs.
          Economic impact is evaluated on model  plants whose description is based
     on representative characteristics of new  or  expanded plants, such as produc-
     tion capabilities,  asset  size, and other  financial measures.  The model
     plants provide  an indication  of the  degree of impact on all new plants in
    .the industry by incorporating into the models the major characteristics
     prevailing in various size segments  of the metallic mineral processing
     industry.   They do not  represent any particular existing plant as any indi-
     vidual plant may  differ in one or more of  the above characteristics.
          The methodology employs  a screening  analysis based on the percentage
     price increase  necessary  to  completely pass-through to customers the added
     cost of  the most  costly regulatory alternative for each plant size.
    
                                         9-105
    

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        ,9.2.2.1  Screening Analysis.  The screening analysis  is  based  on
    the percentage price increase necessary to completely pass through  to
    customers the added cost of the most costly regulatory alternative.  The
    prices used are typically those prices shown in Section 9.1 for  the indivi-
    dual price histories of the metals.  Prices are as of October 1979,  the  same
    date as for the control costs.  The price cited for each metal  is for  the
    first product form that is normally sold in significant quantities  and has  a
    published price.  The prices cited are at the refined metal stage of the
    production process, or contained metal, for, aluminum, copper,  gold, lead/
    zinc, and silver.  The price for iron ore is in the form of pellets at Lake
    Superior mines.  The prices for molybdenum, titanium/zirconium,  tungsten, and
    uranium are in the concentrate form rather than the refined metal form.  The
    differences are a reflection of the differences in the degree of integration
    of the producers of the various metals and the related commercial activity of
    the marketplace.  For example, approximately 62 percent of the copper  that  is
    smelted domestically is part of an integrated operation (U.S. E.P.A.,  1980  p.
    9-5).
         The model plant parameters are described in Chapter 6.  For each  model
    plant the total hours of operation per year is multiplied by the capacity
    utilization rate to provide the effective annual hours of operation.  The
    effective annual hours of operation are then multiplied by the hourly capa-
    city of the plant to provide the tons of ore processed annually at the plant.
    The tons of ore processed annually is then multiplied by the ore grade and
    recovery rate and the result is the product output, or "yield", of the plant.
    In order to simplify the analysis and to be conservative,  a single ore grade
    is employed for each metal, and no byproducts or coproducts are  included
    (except lead/zinc and titanium/zirconium).       .-;•
         The calculations for a copper model plant  are provided as  an example:
    
                                 Copper (150) TPH
               8,500   total hours of  annual operation
               x  96%  capacity utilization rate
               89160   effective  hours of  annual operation
                 150   tons  per hour (TPH)
            x  8..160   hours of operation  per year
           1,224,000   tons  of ore processed per year
    
                                      :•    9-106
    

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           1,224,000   tons per year
            x     .45% ore grade
              5,508   tons of product (contained copper metal)
              5,508   tons of contained copper
              x   93%  recovery rate
              5,122   yield
    
         The yield is calculated for each model plant.  The control costs are
    described in  Section 8.1.  The net incremental annualized control cost above
    the SIP for the most costly regulatory alternative is then divided by the
    yield  to provide the dollar cost increase per unit of product.  The cost
    increase per  unit of product is then divided by the product sales price to
    provide the percentage increase in sales price.  The earlier copper (150) TPH
    model  plant illustration is again used as an example:
    
                                 Copper (150) TPH
    
              5,122    yield in tons
           x  2,000    pounds per ton
         10,244,000    pounds
    
           $372,100    Alternative #3b
           -204,700    less Alternative #1 (SIP)
           $167,400    net incremental annualized cost of Alternative #3b
    
          	=  net incremental annualized cost per pound = 1.6gf per pound
         10,244,000
                1.6ef	incremental cost of Alternative #3b
               95.3d   copper sales price per pound as of October 1979
    = 1.7%
                1.7% = incremental cost of Alternative #3b.
         The percentage price increases for all model plants are shown in Table
    9-62.
                                         9-107
    

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          It  is not unusual for the product prices of many of the ten industries
    to fluctuate by substantially more than two percent.  Further, prices quoted
    among producers of the same metal may frequently vary by two percent or more
    ^due to differences in production costs, transportation costs, inventory
    levels,  contract terms, and so on.  For example, two major copper producers
    follow an announced pricing policy of charging a 2.5 cent premium over the
    Comex quoted copper price (which is greater than 2.5 percent based on a 1979
    price of less than $1.00 per pound).  Also, even in the "worst case" situa-
    tions two percent is considerably lower than the five percent industry average
    rate which is one of the EPA review guideline criteria for major economic
    impact.  Additionally, a two percent cutoff limit was used in the nonmetallic
    minerals NSPS.  Therefore, it appears that a price increase of two percent or
    less could be passed through without adverse impacts on the plants.
    9.2.3  Findings
         This section describes the findings for each of the metals.  Various
    economic factors have different degrees of significance among the ten metals,
    for example imports may be highly significant for one mineral and insig-
    nificant for another.  Therefore, each of the ten metals is discussed
    individually, with emphasis on those economic factors that are most signifi-
    cant to  an assessment of the economic impact of incremental control costs for
    the particular metal at hand.
    9.2.4  Aluminum
         Section 9.1.1 has provided a profile of the aluminum industry and
    Section  9.2.1.2 has noted that the addition of the most costly regulatory
    alternative will require price increases of less than two percent, or speci-
    fically  .03 and .03 percent for the 150 and 300 TPH aluminum model plants.
    Also, the increase in capital for the model plants as a result of the incre-
    mental controls is insignificant for the model plants.  The increased capital
    required for control equipment will add $63,000 and $130,000 to total invest-
    ments of $430,000,000 and $870,000,000 for the 150 and 300 TPH model plants,
    respectively,.  If an investment in an aluminum processing plant would other-
    wise be  accepted, neither the additional price increase nor the additional
    capital  requirement is likely to cause that investment to now be rejected.
                                         9-108
    

    -------
         9.2.4.1  Ownership, Location, Concentration.  There are three principal
    corporations  in the domestic  aluminum industry: Aluminum Co. of America,
    Reynolds Metals Co., and Kaiser Aluminum and Chemical Corp.  These three
    producers are fully integrated and as a group accounted for 86 percent of
    domestic primary aluminum capacity in 1979.  The principal processing states
    are Texas and Louisiana.
         The large size of the corporations in the aluminum industry, as well
    as the small  sizes of the control capital requirements for the model plants,
    indicates that the necessary  capital for the incremental controls will be
    available.
         9.2.4.2.  Pricing.  The  price of aluminum metal has increased from 55
    cents per pound in early 1979 to 58 cents in mid 1979.  During early 1980
    the price continued to increase to 66 cents per pound.
         The incremental control  costs will require a price increase, for the 150
    and 300 TPH aluminum model plants, of less than .1 cent per pound, based on
    an October 1979 sales price of 60 cents per pound.
         In past  years during periods of over capacity the industry has experi-
    enced some discounting from the quoted price as well as some premium pricing
    .when supply is constrained.
         Beyond the normal elements that influence the price of any product, an
    additional element influencing the price of aluminum is that the industry's
    domestic prices are currently subject to the voluntary wage and price guide-
    lines and as  a result there is some disparity between domestic prices and
    world prices  (The Wall Street Journal, May 6, 1980 p. 2).  (As of this writing
    the guidelines are due to expire on December 31, 1980).
         9.2.4.3  Supply.  The aluminum industry is dominated by a relatively
    small number of major participants.  Also, government actions play a sub-
    stantial  role in the aluminum industry and the supply of aluminum.  Six
    international corporate groups (three domestic and three foreign) own or
    control approximately 50 percent of the world's productive capacity.  Another
    50 firms, most nonintegrated and many associated with one of the above six
    groups or with a government, own or control  25 percent of the world's capacity.
    Governments of 24 countries own or control  the remaining 25 percent of capa-
    city. (Stamper and Kurtz,  1978 p.  1).
                                         9-109
    

    -------
         The activity of governments may also influence the aluminum industry
    through changes in stockpiles.  The U.S. Government maintains  a stockpile of
    various forms of aluminum and through 1977 made sales from the stockpile.
    By the end of 1977 the stockpile of primary metal was essentially depleted.
    (Aluminum Association, 1978, Stamper and Kurtz, 1978 p. 20).
         The United States has large quantities of aluminum resources;  however,
    the costs to use these domestic resources exceed the costs to  use foreign
    bauxite.  Therefore, domestic producers import 90 percent of bauxite
    requirements.
         An additional important source of aluminum in the total supply of
    aluminum is the recycling of aluminum scrap.  Domestic secondary recovery of
    aluminum accounted for approximately 22 percent of the total supply of
    domestic aluminum in 1978.
         Primary aluminum metal production requires large amounts  of electrical
    energy, particularly at the smelting stage of the production process.  The
    cost of electrical energy has risen considerably in recent years, parti-
    cularly in the Northwestern United States.  The domestic cost  and availability
    of electricity will play an increasingly important role in the continued
    operation of existing facilities and in the location of new.facilities, both
    domestic and foreign (Chemical Week, 1980 p. 17).
         9.2.4.4  Demand.  Roughly 88 percent of the total aluminum consumption
    in 1978 was in the form of metal.
         The aluminum industry is currently experiencing renewed financial strength
    after several years of surplus capacity and depressed earnings.  A principal
    reason for the improved outlook for the industry is the increased substitution
    of aluminum for steel by the transportation industry in order  to reduce vehicle
    weight and increase fuel  efficiency.
         From 1968 to 1977 domestic demand for primary aluminum grew at an average
    annual  rate of 3.3 percent.  As noted in Section 9.1.1 the domestic demand
    for aluminum is projected to increase at the rate of 2.1 percent per year
    through 1985.
    9.2.5  Copper
         A profile of the copper industry was provided in Section  9.1.4.  Table
    9-83 shows that the addition of the most costly regulatory alternative re-
    quires price increases of 1.7 and 0.8 percent for the 150 and  600 TPH model
    plants, respectively.  The increase in capital for-the model plants as a
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    result  of the  incremental controls  is  .2 percent for both model plant sizes.
    The  increased  capital required for  control equipment will add $161,000 and
    $323,000 to total  investments of $65,000,000 and $133,000,000 for the 150 and
    600  TPH model  plants, respectively.  If an investment in a copper ore proces-
    sing plant would otherwise be accepted, neither the additional cost increase
    nor  the additional capital requirement is likely to cause that investment to
    now  be  rejected.   Although both plants are below the two percent limit, the
    percentage price 'increase for the 600 TPH is substantially lower than the per-
    centage price  increase for the 150  TPH.  This suggests that the added control
    costs may influence new investments toward larger plant sizes.Also, a
    higher  ore grade,  or the addition of byproduct revenues such as nickel or
    silver, or both, would increase revenues and profits for the model plants and
    reduce  the impact  of the control costs.
         9.2.5.1   Ownership, Location,  Concentration.  As noted in Section 9.1.2,
    there are eight leading companies in the copper industry which control 76
    percent of the capacity.  The leading companies are major corporations, most
    of which are fully integrated from mining through refining.  Also, several of
    the  leading companies are prominent in the mining of other metals discussed
    here.   Other major corporations, such as major oil  companies, either directly
    or through subsidiaries, maintain considerable ownership interests in the
    primary copper producing companies both in the United States and in foreign
    countries.  A  partial list of leading copper companies that are owned by
    parent  corporations would include:  Anaconda Company — a subsidiary of ARCO;
    Duval Corporation -- a subsidiary of Pennzoil Company; Magma Copper Company
    -'- a subsidiary of'Newmont Mining Company; and Cyprus Mines Corporation — a
    subsidiary of  Standard Oil Company  (Indiana).  The major copper-producing
    states  are Arizona, Nevada, New Mexico, and Utah.
        9.2.5.2  Pricing.  The price of copper can be volatile.  During December
    1978 the price of copper metal averaged 70.9 cents per pound while one year
    later during December 1979 the price averaged $1.05 per pound for a gain of
    48.7 percent.  Also, during early 1980 the price of copper rose to a record
    high price of $1.41 per pound and then declined to  88 cents per pound by
    April 1980,  a decline of 37.5 percent.
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         Copper is a widely-traded world metal  with  the  bulk  of trading taking
    place on two major international  exchanges:  the New York Commodity Exchange
    (Comex) and the London Metal  Exchange '(L.ME).
         Prior to 1978, U.S. producers followed a pricing policy  not tied  dir-
    ectly to the major exchanges.  The U.S.  producer price was intended to be
    more stable than the exchange price and thereby promote improved business
    planning by participants in the industry.  When  the  exchange  price was high,
    the producer price was normally lower,  and when  the  exchange  price was low,
    the producer .price was normally higher.
         In May 1978 two major U.S.. copper  producers, Kennecott and Anaconda,
    introduced a new pricing policy for their companies  and began basing their
    price directly on the exchange price and charging a  2.5 cent  premium above
    the Comex price.  The new pricing policy permits these two producers to
    compete more effectively with foreign imports by introducing  greater flexi-
    bility into their pricing policy.    The domestic price of copper  was  subject
    to price controls from June 1973 until  May 1974.  Another result  of  the
    change in pricing policy is that domestic copper prices are less  likely to  be
    subject to federal wage and price guidelines, since  the price of  copper is
    determined as a widely-traded commodity.
         9.2.5.3  Supply.  The average U.S. dependence on imports of  copper is  12
    percent. However, the U.S. dependence on foreign imports has varied from a
    position of 20 percent dependence in 1974 to net exporter in 1975, back to  a
    position of 19 percent dependence in 1978.       '••
         An important source of copper in the total  supply of copper is the re-
    cycling of copper scrap.  During 1979 total scrap (new and old)  provided
    approximately 20 percent of total refined copper production at domestic
    primary plants (U.S. Bureau of Mines, MIS).
         Over 40 percent of the Free World's primary copper production is govern-
    ment-owned or controlled.  (Kennecott Copper Corporation, 1979,  p.4).   There-
    fore,  international political  and economic events can have a significant
    impact on the price and supply of copper both in the United States and
    world-wide.  For example, some less-developed countries  that are copper
    exporters have a critical need for foreign currency such  that these countries
    are willing  to continue to sell  copper  on  the world market even during
    periods of over-supply or slack  demand  (The Wall Street  Journal, February 25,
    1980).  Another example of the influence of political events on the supply of
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     copper  is  provided  by the fact  that  in the past U.S. companies have experi-
     enced partial or complete nationalization of their interests in a number of
     countries,  including  Chile,  Zambia,  and Peru.
         9.2.5.4  Demand.   Electrical  applications account for more than half of  '
     domestic copper consumption.  Other  major applications are in the construction,
     industrial  machinery,  and transportation,industries.
         As noted in Section 9.1.4, the  demand for copper is projected to increase
     at  an annual rate of  approximately three percent through 1985.
     9.2.6   Gold
         Section 9.1.5  has provided a  profile of the gold industry and Section
     9.2.1.2 has noted that the addition  of the most costly regulatory alternative
     will require price  increases of less than 2 percent, or specifically .2
     and  .1  percent for  the 75 and 150  TPH gold model plants, respectively.  The
     increase in capital for each of the model plants as a result of the incremen-
     tal  controls is .2  percent.  The increased capital required for control
     equipment  will add  $65,000 and  $93,000 to total investments of $34,000,000
     and  $52,000,000 for the 75 and  150 TPH model plants, respectively.  If an
     investment  in a gold ore processing plant would otherwise be accepted,
     neither the additional  price increase nor the additional capital requirement
     is  likely  to cause  that investment to now be rejected.
         9.2.6.1  Ownership, Location, Concentration.  As noted in Section 9.1.5
     there .are  17 domestic  gold ore  processing plants.  The plants are located
     principally in the  states of Nevada, California, Colorado, South Dakota, and
     Washington.  There  are four leading companies in the industry and these four
     companies  own 70 percent of the industry's capacity.
         9.2.6.2  Pricing.  Gold's  unique position in international financial
     markets has been accompanied by a  history of substantial government control
     over and involvement in the gold market.  This has the effect of making the
     price of gold relatively more dependent on political developments and rela-
     tively less dependent  on economic  fundamentals.
         In recent years the price of  gold has been volatile.   Gold is widely
     regarded as a hedge against economic uncertainty and international political
     turmoil, and therefore during such times the price of gold frequently experi-
     ences sharp price increases,  due to speculation.  The price of gold has  risen
    from $36.41 per troy ounce in 1970 to $800 per troy ounce in early 1980
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    while later declining to about $500 per troy ounce.   During this time
    daily price fluctuations of $20 per ounce or more  have  not been uncommon.
         These price fluctuations can be viewed in relation to the incremental
    control cost price increases of 84 cents per troy  ounce and 52 cents per troy
    ounce, which is equivalent to .2 and .1 percent for  the 75 and 300  TPH model
    plants, respectively.  These price increases are based  on  a gold price of
    $353.44 per troy ounce in October 1979 which is a  conservative price when
    compared to a more recent price of approximately $553 in March of 1980.
         9.2.6.3  Supply.  Government activities play  a  significant role in the
    supply of gold.  It is estimated that nearly half  of all the  gold that has
    been mined in the world, or 1.3 billion ounces, is in government vaults.
         In the United States roughly 40 percent of total output  is  a byproduct
    of base metal mining, particularly copper.  This byproduct relationship
    creates a degree of dependence for the domestic supply of  gold on the out-
    look for copper and other base metals.
         The U.S. relies on imports to supply approximately 50 to 60  percent
    of domestic consumption.  The major source of supply of imported  gold  into
    the United States is the Republic of South Africa.  The Republic  of South
    Africa produced 72 percent of the output of the market economy countries.
    The political controversy surrounding the Republic of South Africa  introduces
    an element of uncertainty into the supply of gold.
         9.2.6.4  Demand.   Jewelry is the dominant fabricated use for gold, fol-
    lowed  by industrial uses, principally in the manufacture of electronic  compo-
    nents, and dentistry.   This  pattern is  likely to continue into the future.
         As stated in Section 9.1.5  the industrial demand for gold is projected
    to grow at an annual rate of  2.7 percent through 1985.  Speculative demand,
    in addition to industrial demand,  is likely to remain  an important element in
    the total demand for gold.
    9.2.7  Iron Ore
          Section 9.1.6 has  provided  a  profile  of  the  iron  ore industry, and
    Section 9.2.1.2 has  noted  that the  addition  of the most costly regulatory
    alternative will  require  price  increases  of  .2  and  .3  percent for  the 1,200
    and 2,400 TPH  iron ore  model  plants, respectively.   The increase in capital
    for the model plants  as a  result of the incremental  controls is less than
     .1 percent.  The  increased  capital  required  for control equipment  will add
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    $444,000 and $1,013,000 to total investments of $707,000,000 and  $1,430,000,000
    for the 1200 and 2400 TPH model  plants, respectively.   If  an investment  in  an
    iron ore plant would otherwise be accepted, neither the additional  control.
    costs nor the additional, capital requirement is likely to  cause that  investment
    to now be rejected.
         9.2.7.1  Ownership, Location, Concentration.   As  noted  in  Section 9.1.6
    there are five leading companies in the iron ore industry  which control  56
    percent of the capacity.
         The steel companies are a dominant force in the iron  ore industry.   The
    steel companies are essentially the only consumers of  iron ore  and  they  main-
    tain considerable ownership in the iron ore companies.
         The two major producing states are Minnesota and  Michigan  and  particu-
    larly Minnesota's Mesabi Range.
         9.2.7.2  Pricing.  The standard unit of weight for iron ore is the  long
    or gross ton which is 2,240 pounds.  Published prices  for  pellets are for a
    long ton unit (LTU) which is one percent of a long ton, or 22.4 pounds.   The
    price of an LTU as of October 1979 was 65.5 cents.  The cost of controls will
    add .16 and .18 cents to the price of an LTU for the 1200  and 2400  TPH model
    plant sizes, respectively.
         9.2.7.3  Supply.  Foreign imports of iron ore have grown from  less  than
    five percent of demand in 1953 to approximately one-third  in 1977.  Over half
    of the imports in 1977 came from mines owned, operated, or partially  owned  by
    U.S. mining and steel companies.  Therefore, the major U.S.  companies in the
    iron ore industry are important not only in terms of domestic operations,
    but also in foreign operations,  which is indicative of their significance
    throughout the marketplace for iron ore.
         In addition to the actions of U.S. companies, availability or  price of
    iron ore from abroad may be influenced by foreign political  developments.
    Companies owned or controlled by foreign governments produced about 60
    percent of the estimated 785 million tons of iron ore  produced  outside of
    the United States in 1977.  For example, nationalization of  U.S.-owned mines
    in Chile in 1971 and in Venezuela and Peru in 1975 affected  -about one-third
    of U.S. imports of iron ore.  Imports from Chile dropped to  a small fraction
    of their original level for several years; imports from Peru ceased for  a
    year and a half; imports from Venezuela in 1977 were less  .than  50 percent
    of their volume in 1975.  (Klinger, 1978 p. 3, 19).
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          9.2.7.4  Demand.   More than 98 percent  of  the  iron ore consumed in the
     United States is used  in the production  of  iron and  steel.  Therefore the
     financial  condition of the iron ore industry is dependent upon the financial
     condition  and production plans of the  steel  industry.
          As stated in Section 9.1.6 the steel  industry  is projected to maintain
     good growth through 1985, with demand  for  iron  and  steel increasing at an
     annual rate of 2.5 percent.
     9.2.8  Lead/Zinc
          A profile of the  lead and zinc, industries  was  provided in Sections 9.1.7
     and  9.1.1.5.   As in earlier sections,  lead  and  zinc  are considered jointly for
     this discussion since  they are often mined  as byproducts and coproducts.  Table
     9-83 shows that the addition of the most costly regulatory alternative will re-
     quire a price increase of .2 percent for both the 300 and 600 TPH lead/zinc
     plants.  The  increase  in capital  for the model  plants, as a result of the
     incremental controls,  is .2 percent for both model plant sizes.  The increased
     capital  required for control  equipment will  add  $212,000 and $323,000 to total
     investments of  $95,000,000 and $214,000,000 for  the  300 and 600 TPH model plants,
     respectively.   If an investment in  a lead/zinc  ore processing plant would
     otherwise  be  accepted,  neither the  additional control costs nor the additional
     capital  requirements are likely to  cause that investment to now be rejected.
          9.2.8.1  Ownership,  Location,  Concentration.  As noted in Sections 9.1.7
     and  9.1.1.5, there  are  eight  leading companies  in the lead/zinc industry.
     These  eight companies control  85  percent of the  industry's capacity.
         The major  lead  and  zinc  primary producers  are large corporations that
     are  vertically  integrated from mining through refining.   Several  of the major
     producers  are also  prominent  in the mining of other rnetals among the fifteen
    metals discussed  here.   Many  of the  leading producers also have substantial
    foreign  interests.
         Except for the  lead  deposits in the Virburnum Trend in southeastern
    Missouri, the largest lead-producing area in the United  States, the value of
    associated metals often  exceeds the value of the lead.  The principal  proces-
    sing states are Missouri,  Idaho,  Colorado,  Utah, and New Jersey.
         9.2.8.2  Pricing.   During  early and mid-1979, both  lead  and  zinc experi-
    enced increasing prices with  lead rising from 40.8 to a  high  of 61.1 cents
    per pound and zinc rising from 34.6 to a high of 39.4 cents per pound.   Late
    in 1979 and during early 1980, prices of both metals began to  decline,  with
    lead falling below 49 cents per pound and zinc falling below  38 cents  per pound.
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         Both metals are commonly traded internationally,  with  the  LME  serving  as
    the most widely followed exchange.
         United States government actions can be a significant  force in the
    market for both lead and zinc.  Lead was subject to domestic price  controls
    from June 1973 to December 1973.  Zinc was subject to  price controls from
    August 1971 to December 1973.
         The price increases are .1 cent per pound for both the 300 and 600  TPH
    model plants.  This price increase is equivalent to .2 percent.
         9.2.8.3  Supply.  Foreign imports of lead comprise roughly 10  to 20
    percent of consumption.  Foreign imports of zinc account for roughly 60  per-
    cent of domestic consumption (Commorata, 1978 p. 1).  The composition of zinc
    imports has changed over the past decade from predominantly ore and concen-
    trate with metal playing a lesser role, to zinc imports which are now predomi-
    nantly metal, with ores and concentrates now accounting for the lesser share.
         The significance of the change in the composition of zinc  imports is
    that as less of the product's value is added in the U.S., less  domestic  zinc
    smelting and refining capacity is needed.  From December 1968 to May 1975,
    eight primary zinc smelters or refineries closed in the United  States due to
    either obsolescence, or lack of concentrate feed materials, or  environmental
    costs, or some combination of these elements (one plant was converted'to an
    eletrolytic process and a second plant was purchased by another company  and
    reopened in 1973) (International Trade Commission, 1978 p.  A-24).  These
    closings represented a decline in domestic capacity of about 570,000 short
    tons, or approximately 50 percent of domestic capacity (International Trade
    Commission, 1978 p. A-24, Commorata, 1978 p. 1).  An additional zinc smelter
    closed in December 1979 (The Wall Street Journal, April 16, 1980).
         Recycled lead is an important component of supply accounting for about
    35 to 40 percent of lead consumption (Ryan and Hague,  1977  p. 1).  Relative
    to recycled lead, recycled zinc is less important accounting for only about
    five percent of the total U.S. supply because much of  zinc's consumption is
    in dissipative uses (Commorata, 1978 p. 1)
         The U.S. government maintains a stockpile of both lead and zinc. Sales
    from the stockpile have had a substantial impact on both industries, particu-
    larly from 1972 through 1974 when sales from the stockpile  accounted for 3,
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     13.2,  and 17.4 percent of  total  domestic  lead demand and 12.4, 16.5, and 18.7
     percent of total  domestic  zinc demand  (Ryan  and  Hague, 1977 p. 11, Commorata,
     1978 p. 14).
          9.2.8.4  Demand.   The largest  use of lead is  in storage batteries (61
     percent), particularly automobile batteries  which  contain about 20 pounds of
     lead.   Other major uses of lead  are as a  gasoline  additive,(12 percent), elec-
     trical uses (2 percent), paints  (6  percent), ammunition (4 percent), construc-
     tion (3 percent), with the remainder divided among a variety of other uses.
          The principal uses of zinc  are in galvanized  steel products for the
     construction industry  (40  percent)  and transportation  industry (26 percent)
     in electrical equipment (12 percent),  in  machinery and chemicals (10 percent)
    , and other uses (12 percent).   The demand  for zinc  in galvanizing has been
     growing, while the demand  for zinc  in  diecasting has been declining in favor
     of aluminum and plastic.  ,
          Lead is faced with environmental  problems in  several areas relating to
     both-its production and consumption.  For example,  lead smelters have a number
     of environmental  problems.  The  increased use of "unleaded" gasoline is
     lowering demand for lead in this application.  Also, lead is no longer used
     in interior paints due to  its harmful  effects when children ingest the paint.
     Additionally, the use  of lead shot  for waterfowl hunting is being replaced by
     the use of steel shot in order to prevent  lead poisoning of aquatic life.
          Over the past decade  the demand for  lead has  grown by 3 percent per year
     while  the demand for zinc  has been  stable.   Through 1985 the demand for lead
     and zinc is projected  to increase at an annual rateof  one to two percent per
     year due primarily to  the  growth in demand for lead-acid storage batteries.
     9.2.9   Molybdenum
          Section 9.1.8 has provided  a profile of the molybdenum industry, and
     Section 9.2.1.2 has noted  that the  addition  of the most costly regulatory
     alternative will  require price increases  of  less than  2 percent, or specifi-
     cally .1 percent for both  the 300 and  1200 TPH molybdenum model plants.
     Also,  the increase in  capital for both of the model plants as a result of
     the incremental controls is .2 percent.  The increased capital required
     for control equipment  will add $213,000 and  $464,000 to total investments
     of $100,000,000 and $285,000,000 for the  300 and 1200  TPH model plants,
     respectively.  If an investment  in  a molybdenum  ore processing plant would
     otherwise be accepted, neither the  additional price increase nor the
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     additional  capital  requirement is likely to cause that  investment  to  now be
     rejected.
          9-2.9.1  Ownership,. Location,  Concentration.   As noted  in Section 9.1.8
     two corporations mine deposits primarily for molybdenum.  The principal firm
     is the Climax Molybdenum Co.,  a division of Amax  Inc. and the other firm is
     Molycorp.  Inc.,  which was acquired  in  1977  by Union Oil Co.  of California.
     Additionally, Duval  Copper,  a  subsidiary of Pennzoil Co., and Kennecott Corp.
     recover a  significant amount of molybdenum  from their copper mining operations,
          Two major corporations, neither of  which has  historically been a signifi-
     cant participant in  the  molybdenum  industry,  have  recently begun ambitious
     expansion  programs  in the molybdenum industry.  The two companies  are Standard
     Oil  Company (Indiana), through its  Cyprus Mines subsidiary,  at the Thompson
     Creek molybdenum mine in Idaho;  and Atlantic  Richfield, through its Anaconda
     subsidiary,  at the Liberty mine in  Nevada.
          9.2.9.2  Pricing.   The  price of molybdenum has increased twelve times
     since early 1974 and  each price increase has  been  from 5 to  16 percent over
     the  previous level.   The actual  price  has risen considerably for molybdenum
     concentrate  to $8.84  as  of October  1979.  The incremental cost price increases
     are  1.1  and  .6 cents  per pound for the 300  and 1200 TPH model plants respec-
     tively.  The control  cost price  increases are equivalent to  percentage price
     increases of  .1  percent  for  both  model plants, which can be  viewed in relation
     to historical  percentage price increases of from 5  to 16 percent.
          9.2.9.3  Supply.  In 1977 the world mine output of molybdenum contained
     in concentrate was an estimated 206 million pounds.  Three countries, the
     United States, Canada, and Chile  provided 89  percent of the  total  of which
     the  United States provided approximately 60 percent.  Historically, the
     United States  is the world's leading producer and  is a net exporter of molyb-
     denum.  Approximately one-half of the  U.S. domestic production is  exported.
          In the  past the U.S. Government has maintained a stockpile of molybdenum.
     By yearend 1977  the U.S.   Government stockpile was fully depleted.   Domestic
     reserves and production  capacity  are currently considered adequate to supply
     national emergency needs  and thus no new government stockpile purchases are
     anticipated.
         The dominant position of the United States in the world  molybdenum
     industry and the element of stability associated  with a domestic source of
     supply creates a favorable set of circumstances for both the  producers and
    consumers of molybdenum.
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         9.2.9.4  Demand.  The major end use for molybdenum  is  in  the  production
    of molybdenum containing steels.  The steel  industry consumes  approximately
    70 percent of domestic molybdenum production.
         The molybdenum industry is experiencing a tight supply/demand balance.
    Molybdenum demand exceeded supply in 1979 for the sixth  time in  the last
    seven years, although the expansion programs noted above plus  others,  should
    serve to moderate the tight supply demand balance.  As discussed in Section
    9.1.8 the demand for molybdenum is projected to increase at a  rate, of  approxi-
    mately five percent annually through 1985.
    9.2.10  Silver                   .   .
         Section 9.1.10 has provided a profile of the silver industry, and
    Section 9.2.1.2 has noted that the addition of the most  costly regulatory
    alternative will require price increases of .5 and .2 percent  for  the  50
    and 150 TPH model plants, respectively.  The increase in capital for the
    model plants as a result of the incremental controls is  .4  and .2  percent,
    respectively.  The increased capital required for control equipment will  add
    $92,000 and $126,000 to total investments of $25,000,000 and $76,000,000  for
    the 50 and 150 TPH model plants, respectively.  If an investment in a  silver
    processing plant would otherwise be accepted neither the additional price
    increase nor the additional capital requirement is likely to cause that
    investment to now be rejected.
         ,9.2.10.1  Ownership, Location, Concentration.  As  noted in  Section
    9.1.10, there are five leading companies in the silver  industry  which  control
    85 percent of the capacity.  The two principal producing states  are Colorado
    and Idaho, particularly the Coeur d'Alene mining district in Idaho.
         9.2.10.2   Pricing.  The price of silver has experienced  sharp fluctua-
    tions recently.  During December 1978 the price of silver averaged $5.93  per
    troy ounce while one year later, during December 1979,  the price averaged
    $21.79 per troy ounce for a gain of more than 350 percent.   The  price  of
    silver continued to rise during early 1980 to more than  $40 per  ounce  and
    then declined over a period of weeks to approximately $13 per ounce.  The
    sharp price fluctuations were largely the result of the  trading  activity  of
    speculators on the commodity exchange.
         The incremental control costs will require price increases  of 7 cents
    and 3 cents per troy ounce for the 50 'and 150 TPH silver model plants.  The
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    price  increases are equivalent to percentage price increases of .5 and .2
    percent  based on  an October  1979 silver price of $13.89 per troy ounce.
         9.2.10.3  Supply.  About 70 percent of silver mined is produced"as a
    byproduct  of copper mining as well  as  lead and zinc mining (Drake, 1978 p.
    10).   As a result, the  supply of silver provided by domestic production is
    dependent  on the  outlook for other  metals..
         A second important source of supply of silver is. foreign imports.
    Foreign  imports normally supply approximately 40 percent of consumption.
         The United States government maintains a silver stockpile although sales
    from or  purchases for the stockpile-have not been significant for a number of
    years  (Drake, 1978 p. 1, 9).
         9.2.10.4  Demand.  As mentioned above, the trading activity of specu-
    lators on  the commodity exchange can play a major role in the price and
    demand for silver.  The major industrial use of silver is for photography,
    consuming  39 percent of domestic demand in 1979.  Other principal  uses are
    electrical  and electronic components which accounted for 25 percent, and
    silverware, which accounted for 15  percent, with the remainder used in a
    variety  of  other products.
         In  spite of progress in some special areas to develop substitutes for
    silver,  no satisfactory substitute  exists for most of silver's uses (Drake,
    1978 p.  12, Chemical Week, February 27, 1980 p. 15).   Also, the demand for
    silver has  risen faster than the world supply for most of the last decade
    (Drake,  1978 p.  8).  Therefore, the general lack of close substitutes for
    silver,  plus the fact that demand is outpacing supply suggests that the incre-
    mental  control costs could be passed through to consumers (Chemical Week, 1980)
         Demand for silver is projected to increase at an annual  rate  of three
    percent  through 1985.
    9.2.11   Titanium/Zirconium
         A profile of the titanium industry was provided  in Section 9.1.11 and a
    profile  of the zirconium industry was provided in Section-9.1.16.   Table 9-83
    shows that the addition of the most costly regulatory alternative  will
    require  price increases of .8 percent each for the 300 and 600 TPH titanium/
    zirconium model  plants.   Also, the  increase in capital  for the model  plants
    as a result of the incremental controls is .9 and 1.2 percent, respec-
    tively.  The increased capital required for control  equipment will add
    $92,000  and $203,000 to total investments of $10^,000,000 and  $17,000,000 for
                                         9-121
    

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    the 300 and 600 TPH model plants, respectively.   If  an  investment  in  a
    titanium/zirconium processing plant would otherwise  be  accepted, neither the
    additional price increase nor the additional  capital  requirement is likely to
    cause that investment to now be rejected.
         9.2.11.1  Ownership, Location, Concentration.   As  noted  in Section 9.1.11
    there are essentially only three companies in the titanium/zirconium  (sand)
    industry, Asarco, Inc., Humphreys Mining Company, and E.I.  DuPont  deNemours &
    Co., Inc.  These three companies own four ore processing  plants.   The
    principal processing states are Florida, Georgia, and New Jersey,,
         9.2.11.2  Pricing.  The price for rutile ore was $375-$400 per short ton,
    as of October 1979, or. 18.8 cents to 20 cents per pound.   The price for
    zirconium ore (65 percent ZrOg) was $150 per  short ton, or 7.5 cents  per
    pound (EMJ Nov. 79 p. 21).  Assuming 50 percent  of the  processing  plant's
    output is titanium and 50 percent of the processing  plant's output is zir-
    conium, the average price of the two products combined  is approximately 13.2
    cents per pound (18.8 + 7.5 = 26.3 * 2 = 13.2).
         9.2.11.3  Supply.  As discussed in Section  9.1.11  the mineral sources
    of titanium are rutile and ilmenite.  Australia  has large desposits of rutile
    that supply much of the United States demand  (the exact percent of demand
    supplied by imports is proprietary).  The large  Australian rutile  deposits
    present formidable economic competition for domestic deposits.
         9.2.11.4  Demand.  Approximately 98 percent of the demand for titanium
    is for consumption in the form of titanium dioxide pigment for use in paint
    and paper coatings.  The remaining demand for titanium  is-consumed in the
    form of titanium sponge metal for use primarily  in aerospace applications.
    9.2.12  Tungsten
         A profile of the tungsten industry was provided in Section  9.1.12.
    Table 9-62 shows that the addition of the most costly regulatory alternative
    will require a price increase of .5 percent for  the 25  TPH tungsten plant.
    The increase in capital for the model plant as a result of the incremental
    controls is one percent.  The increased capital  required  for control  equip-
    ment will add $46,000 to a total investment of $4,400,000 for the  25  TPH
    model plant.  If an investment in a tungsten processing plant would otherwise
    be accepted, neither the additional cost increase nor the additional  capital
    requirement is likely to cause that investment to now be rejected.
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         9.2.12.1  Ownership, Location, Concentration.   As noted  in  Section
    9.1.1.2 there are four active tungsten operations.   There is  one leading
    firm, Union Carbide Corporation, which owns 71 percent of the industry's
    capacity.  The principal tungsten operations are located in California and
    Nevada.
         9.2.12.2  Pricing.  The standard industry unit of measure is the short
    ton unit (STU) which is one percent of a ton or twenty pounds.  The price of
    tungsten expressed on a per pound basis has risen from $4.77 in  1974 to  a
    high of $9.77 in 1977 and then declined to $6.74 in 1979.  The incremental
    control costs will require a price increase of 3.3 cents per pound.
         9.2.12.3  Supply.  Production of domestic tungsten concentrate generally
    supplies from one-third to two-thirds of US. demand (Kornhauser  and Stafford,
    1978 p. 1).  Another important source of supply of tungsten is the U.S.
    government tungsten stockpile.  Sales from the stockpile have been a signi-
    ficant factor in the marketplace over recent years.  For example, during  1979
    the General Services Administration sold 5.6 million pounds of tungsten from
    the government stockpile and released an additional 0.2 million  pounds
    directly to consumers for use in government programs.  This 5.8 million
    pounds released from the government stockpile represents approximately 29
    percent of the total U.S. consumption, estimated at 20.0 million pounds,
    during 1979, and is also typical of the five year average percentage of  27 .
    percent (Thurbur, 1980 p. 187).
         9.2.12.4  Demand.  Tungsten's extreme hardness at high temperatures  is
    its most important characteristic.
         Its major end uses are  in cutting and wear-resisting materials, high-
    speed' and tool and die  steels, superalloys, and nonferrous alloys.
         Demand is projected to  increase  at a rate of five percent per year
    through 1985.
    9.2.13 Uranium
         Section 9.1.13 has provided a profile of the uranium  industry, and
    Section 9.2.1.2 has noted that the addition of the most  costly regulatory
    alternative will require price increases of less than two  percent, or speci-
    fically  .2 and  .1 percent for the  25  and 75 TPH uranium  model plants, respec-
    tively.  ,Also the increase  in capital for the model plants as a result of the
    incremental controls  is  .8  and  .3  percent, respectively.   The increased
    capital required for  control  equipment will add $28,000  and  $38,000 to total
                                          9-123
    

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     investments of  $3,700,000  and  $11,200,000 for the 25 and 75 TPH model plants,
     respectively.   If  an  investment  in  a  uranium processing plant would otherwise
     be accepted, neither  the additional price increase nor the additional capital
     requirement is  likely to cause that investment to now be rejected.
          9.2.13.1   Ownership,  Location, Concentration.  As described in Section
     9.1.13  there are 31 operations located  primarily in the Western states,
     particularly, Colorado, New  Mexico, Wyoming, Utah, and Texas.  There are 10
     leading companies  which own  74 percent  of the industry's capacity.  Several
     major oil  companies are significant participants in the industry, as well as
     other major corporations,  some of which are prominent in the mining of
     several  metals  discussed earlier.
          9.2.13.2   Pricing.  Uranium is marketed, and prices are quoted for
     uranium, in the concentrate  form which  is uranium oxide (U^OQ), commonly
     referred to as  yellowcake.
          From  1972  to  1979 the price of uranium rose 700 percent from roughly $6
     per pound  to over  $40 per  pound.  The sharp increase in prices which began in
     1972  led to widespread allegations that an international uranium cartel was
     causing  the price  increases.   Uranium is normally sold through long term
     contracts.  A major domestic corporation experienced considerable financial
     loss  as  a  result of the price  increase  which the corporation alleges was due
     to the  existence of a cartel.  Several  years ago the corporation signed long
     term  contracts  to  supply uranium that it expected to purchase and deliver in
     the future.  Subsequently, in  1976, the allegations that an international uran-
     ium cartel  was  causing the price increases led to litigation.  The final out-
     come  of the litigation is still  pending; however, it is possible that the
     price of uranium is not primarily the result of the free interaction of
     supply  and  demand.
         A perspective on the relative size of the incremental  control cost price
     increases can be gained by comparing historical  price increases to the incre-
     mental control   cost price increases.  The incremental  control costs represent
     price increases of 8.8 and 3.8 cents per pound for the 25 and 75 TPH model
     plants, which is equivalent to .2 and .1 percent based on a uranium sales
     price of $42.70 per pound in mid-19!79.
         During late 1979 and through the middle of  1980 the price of uranium
    experienced weakness,  declining to approximately $30.00 per pound.  At a more
                                         9-124
    

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    current price of $30.00 per pound, few domestic operations are profitable,
    regardless of pollution controls.  However, at a price of $30.00 per pound
    the incremental control costs continue to represent modest price increases  of
    .3 and .1 percent, respectively.
         9.2.13.3  Supply.  The sharp increases in the price of uranium over
    recent years, from $6 to $40 per pound, has stimulated new uranium mining
    activity.  Also  world inventories of uranium are high; currently at a level
    sufficient to meet requirements for two years.  Both Canada and Australia
    contain substantial deposits of low cost uranium, and Africa is increasing
    its production capacity.  An indication of the high level of inventories and
    the certainty of supplies is provided by the fact that when prices were
    recently at higher levels some utilities were liquidating portions of their
    inventories.  Therefore supplies of uranium should be more than adequate
    through 1985.
         A significant additional element that determines the supply of uranium
    for domestic uses is United States Government policy.  Congress is discussing
    the idea of reducing imports of uranium.  Imports are approximately 8 percent
    of total  U.S. consumption and growing.  Imports of uranium were banned from
    1964 to 1976 when there also were large supplies.  Currently,  imports are
    restricted to 30 percent of the uranium that is enriched to become nuclear
    fuel, but imports will be allowed to rise to 100 percent by 1984 (The Wall
    Street Journal, May 28, 1980).
         9.2.13.4  Demand.  Roughly 98 percent of the demand for uranium is for
    use in the production of nuclear energy.  There are no substitutes for
    uranium in the production of nuclear energy 'and since nuclear power provides
    about 12.5 percent of total U.S. electricity needs this suggests a continuing
    demand for uranium.
         Current issues concerning the future of nuclear energy production,
    underscored by the accident at Three Mile Island, plus slower growth in the
    total demand for electricity, create considerable uncertainty in projections
    of the demand for uranium.  Projections made in July 1978 of the annual
    uranium requirements of U.S. utilities for the years 1980 through 1986, were
    reduced as of December 1979 by an average annual  amount of approximately 18
    percent (White, 1980).
                                         9-125
    

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    9.3  SOCIO-ECONOMIC IMPACT ASSESSMENT
         The purpose of Section 9.3 is to address those tests of macroeconomic
    impact as presented in interim guidelines for Executive Order 12291 and,
    more generally, to assess any other significant macroeconomic impacts that
    may result from the NSPS.
         The economic impact assessment is concerned only with the costs or
    negative impacts of the NSPS.  The NSPS will also result in benefits or
    positive impacts, such as cleaner air and improved health for the population,
    potential increases in worker productivity, increased business for the
    pollution control manufacturing industry, and so forth.  However, the NSPS
    benefits will not be discussed here.
         There are three principal rev.iew criteria to determine significant
    macroeconomic impact.
         1.   Additional annual costs of compliance, including capital charges
              (interest and depreciation), total $100 million (i) within any one
              of the first five years'of implementation, or (ii) if applicable
              within any calendar year up to the date by which the law requires
              attainment of the relevant pollution standard.
         2.   Total additional cost of production of any major industry product
              or service exceeds 5 percent of'the selling price of the product.
         3.   The Administrator requests such an analysis (for example when
              there appear to be major impacts on geographical regions or local
              governments).
         The metallic minerals NSPS will not trigger any of the above tests.
    The metal that will experience the highest annual costs of compliance is
    iron ore with one;projected 1,200 TPH plant and one projected 2,400 TPH
    plant.  The plants will have costs of compliance of $420,100 and $872,400
    or a total of $1,292,500, which is far below the $100 million test.
    Further, Table 9-63 shows that even if the costs of compliance for each of
    the ten metals are summed, the grand total is $4,555,000; or far below the
    $100 million test.  Also, Table 9-62 has shown that all of the metals are
    well below the test of an increase in costs of 5 percent of the selling
    price.  Finally, new plants that are subject to the NSPS will be
    diversified geographically.  Therefore, for the reasons given above, no
    significant macroeconomic impacts are likely.
                                    9-126
    

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                  Table 9-63.  SUMMARY OF INDUSTRY ANNUALIZED COST
                    FOR THE MOST STRINGENT REGULATORY ALTERNATIVE
                                    ($ in OOO's)
    Metal
    Aluminum
    
    Copper
    Gold
    
    Iron ore
    
    Lead/Zinc*
    Molybdenum
    Silver
    Titanium/
    Zirconium
    (sand)
    Tungsten
    Uranium
    GRAND TOTAL
    Plant
    (Mg/hr)
    140
    270
    140
    540
    68
    140
    1,100
    2,200
    270
    540
    270
    1,100
    45
    140
    270
    540
    
    23
    23
    68
    
    size
    (ton/hr)
    (150)
    (300)
    (150)
    (600)
    (75)
    (150)
    (1,200)
    (2,400)
    (300)
    (600)
    (300)
    (1,200)
    (50)
    (150)
    (300)
    (600)
    
    (25)
    (25)
    (75)
    \ * v J
    Projected
    number of
    new sources
    1
    1
    1
    1
    1
    1
    1
    1
    2
    1
    1
    2
    2
    1
    1
    1
    
    1
    2
    3
    
    Annuali zed
    cost of
    NSPS increment
    $ 53
    95
    167
    303
    66
    82
    441
    867
    174
    264
    218
    464
    76
    108
    102
    156
    
    41
    28
    36
    
    Total
    $ 53
    95
    167
    303
    66
    82
    441
    867
    348
    264
    218
    928
    - 152
    108
    102
    156
    
    41
    56
    108
    $4,555
    *Note the discussion in Section 8.1 on the possible effects of the NAAQS for
     lead on the calculation of the control costs for lead/zinc processing plants.
                                        9-127
    

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                                     REFERENCES
    Aluminum Statistical Review in 1978.  The Aluminum Association p.  29.
    
    Chemical Week.  For Precious metals, it's a mad, mad world.  February 27,
      1980.  p. 15.
    
    Chemical Week.  Power crisis eases in the Pacific Northwest.  November 5,
      1980 p. 17.
    
    Commorata, V, Anthony.  May 1978.  Zinc:  Mineral Commodity Profile.  U.S.
      Bureau of Mines.  Washington, D.C. P. 1.
    
    Drake, Harold J., September 1978.  Silver:  Mineral Commodity Profile.  U.S.
      Bureau of Mines.  Washington, D.C.  p. 1, 8, 9, 10, 12.
    
    International Trade Commission.  Unalloyed, Unwrought Zinc.  USITC Publi-
      cation 8949 June 1978 p. A-24, A-4.
    
    Kennecott Copper Corporation.  SEC Form 10-K.  December 31, 1979,  p. 4.
    
    Klinger, F.L«  May 1978.  Iron Ore:  Mineral Commodity Profile.  U.S. Bureau
      of Mines.  Washington, D.C.  p. 3 and 19.
    
    Kornhauser, Ben A. and Philip T. Stafford.  September 1978.  Tungsten:
      Mineral Commodity Profile.  U.S. Bureau of Mines.  Washington, D.C. p. 1.
    
    Ryan, J.P. and J.M. Hague.  December 1977.  Lead:  Mineral Commodity Profile.
      U.S. Bureau of Mines.  Washington, D.C. p.'l, 11.
    
    Stamper, John W. and Horace F. Kurtz.  1978.  Aluminum:  Mineral Commodity
      Profile.  U.S. Bureau of Mines.  Washington, D.C. p. 4, 1.
    
    Thurbur, W.C.., Engineering and Mining Journal.  March 1980.  Tungsten:
      Demand Tops Supply Despite GSA Releases,  p. 187.
    
    United States Bureau of Mines.  Mineral Industry Surveys - Copper.  July 1980
      p. 2.
    
    United States Environmental Protection Agency.  Arsenic Emissions from Primary
      Copper Smelters - Background Information.  Section 9.1, p. 9-5.
    
    Wall Street Journal, The.- Poland's Copper and Silver Ore Earning Nation
      Critically Needed Hard Currency.  February 25, 1980.
    
    Wall Street Journal, The.  St. Joe Won't Replace Zinc Smelter It Closed
      Recently in Monaca, Pa.  April 16, 1980.
    
    Wall Street Journal, The.  Reynionds Metals and Kaiser Aluminum Roll Back Price
      Boosts on Some Products.  May 6, 1980 p. 2.
                                         9-128
    

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    Wall Street Journal, The.  Uranium Producers Hope Price Will  Rise On Output
      Cutbacks, Import Restrictions.  May 28, 1980.
    
    White, George Jr., Engineering and Mining Journal.  March 1980.   Uranium:
      Improving Supplies Weaken Price Structure.  P. 195.
                                        9-129
    

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                                        TECHNICAL REPORT DATA
                                (Please read Instructions on the reverse before completing)
    1. REPORT NO,
      EPA-450/3-81-009a and -009
                                                                3. RECIPIENT'S ACCESSION NO.
    4. TITLE AND SUBTITLE
                                                                5. REPORT DATE
      Metallic Mineral Processing Plants - Background
      Information for Proposed Standards
                 6. PERFORMING ORGANIZATION CODE
                                                                    August 1982
    7. AUTHOR(S)
                                                                8. PERFORMING ORGANIZATION REPORT NO.
    9. PERFORMING ORGANIZATION NAME AND ADpRESS
    
      Office of Air Quality  Planning and Standards
      U.S.  Environmental Protection Agency
      Research Triangle Park, North Carolina  27711
                                                                10. PROGRAM ELEMENT NO.
                 11. CONTRACT/GRANT NO.
                                                                  68-02-3063
    12. SPONSORING AGENCY NAME AND ADDRESS
      DAA  for Air Quality Planning and Standards
      Office  of Air, Noise, and  Radiation
      U.S.  Environmental Protection Agency
      Research Triangle Park,  North Carolina  27711
                                                                13. TYPE OF REPORT AND PERIOD COVERED
                  14. SPONSORING AGENCY CODE
                   EPA/200/04
    15. SUPPLEMENTARY NOTES
    16. ABSTRACT
      Standards  of performance  for the control of  particulate matter emissions from
      metallic mineral processing  plants are being proposed under the authority of
      Section 111  of the Clean  Air Act.   These standards would apply to  facilities at
      processing plants for which  construction or  modification began on  or .after the
      date of proposal of the regulation.  This document contains background  .
      information  and environmental  and  economic impact assessments of the  regulatory
      alternatives considered in .developing proposed  standards.
    17.
                                    KEY WORDS AND DOCUMENT ANALYSIS
                      DESCRIPTORS
      Air pollution
      Pollution control
      Standards of performance
      Metallie'mineral  processing plants
      Particulate matter
                                                   I).IDENTIFIERS/OPEN ENDED TERMS  C.  COSATI Held/Group
    Air pollution control
      13B
    18, DISTRIBUTION STATEMENT
    
      Unlimited
    19. SECURITY CLASS (This Report)
     Unclassified
    21. NO. OF PAGES
       822
                                                   20. SECURITY CLASS (This page')
                                                    Unclassified
                                                                              22. PRICE
    EPA Fo»m 2220-1 tR°v. 4-77)   .PREVIOUS FOITION is OBS.OL.ETE
    

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