EPA-600/2-77-227
November 1977
Environmental Protection Technology Series
MANUAL FOR THE CONTROL OF HAZARDOUS
MATERIAL SPILLS: VOLUME I •
Spill Assessment and Water
Treatment Techniques
Laboratory
Office of Research and Development
U.S. Environmental Protection Agency
Cincinnati, Ohio 45268
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RESEARCH REPORTING SERIES
Research reports of the Office of Research and Development, U.S. Environmental
Protection Agency, have been grouped into nine series. These nine broad cate-
gories were established to facilitate further development and application of en-
vironmental technology. Elimination of traditional grouping was consciously
planned to foster technology transfer and a maximum interface in related fields.
The nine series are:
1. Environmental Health Effects Research
2. Environmental Protection Technology
3. Ecological Research
4. Environmental Monitoring
5. Socioeconomic Environmental Studies
6. Scientific and Technical Assessment Reports (STAR)
7. Interagency Energy-Environment Research and Development
8. "Special" Reports
9 Miscellaneous Reports
This report has been assigned to the ENVIRONMENTAL PROTECTION TECH-
NOLOGY series. This series describes research performed to develop and dem-
onstrate instrumentation, equipment, and methodology to repair or prevent en-
vironmental degradation from point and non-point sources of pollution. This work
provides the new or improved technology required for the control and treatment
of pollution sources to meet environmental quality standards.
This document is available to the public through the National Technical Informa-
tion Service, Springfield, Virginia 22161.
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EPA-600/2-77-227
November 1977
MANUAL FOR THE CONTROL OF HAZARDOUS MATERIAL SPILLS
VOLUME ONE
SPILL ASSESSMENT AND WATER TREATMENT TECHNIQUES
by
K. R. Huibregtse, R. C. Scholz, R. E. Wullschleger
J. H. Moser, E. R. Bellinger, and C. A. Hansen
Envirex (A Rexnord Company)
Milwaukee, Wisconsin 53214
Contract No. 68-03-2214
Project Officer
Ira WiIder
Oil and Hazardous Materials Spills Branch
Industrial Environmental Research Laboratory-Cincinnati
Edison, New Jersey 08817
INDUSTRIAL ENVIRONMENTAL RESEARCH LABORATORY
OFFICE OF RESEARCH AND DEVELOPMENT
U. S. ENVIRONMENTAL PROTECTION AGENCY
CINCINNATI , OHIO 45268
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DISCLAIMER
This report has been reviewed by the Industrial Environmental Research
Laboratory-Cincinnati, U.S. Environmental Protection Agency, and approved
for publication. Approval does not signify that the contents necessarily
reflect the views and policies of the U.S. Environmental Protection Agency,
nor does mention of trade names or commercial products constitute endorse-
ment or recommendation for use.
i i
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FOREWORD
When energy and material resources are extracted, processed1, converted, and
used, the related pollutional impacts on our environment and even on our
health often require that new and increasingly more efficient pollution con-
trol methods be used. The Industrial Environmental Research Laboratory,
Cincinnati (lERL-Ci) assists in developing and demonstrating new and improved
methodologies that will meet these needs both efficiently and economically.
This report contains suggested procedures for control of hazardous material
spills using improvised treatment processes. The methods presented should
be used as a last resort in hazardous spill control but do provide an alter-
native treatment approach if more sophisticated equipment is not available.
This Manual includes sections regarding: notification procedures, an inven-
tory of information sources, methods for spill identification and assessment,
a thought guide for determining the best method of handling a spill, plus
suggested treatment schemes for the 303 designated hazardous chemicals, a
limiting factor system design approach, and design, construction and opera-
tion steps for each of the five treatment processes applicable to improvised
systems. The Manual will be updated periodically to insure the contents are
current. Further information on the control of hazardous material spills
may be obtained from the Oil and Hazardous Materials Spills Branch (lERL-Ci),
Edison, New Jersey 08817-
David G. Stephan
Di rector
Industrial Environmental Research Laboratory
Cinci nnat i
i i i
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ABSTRACT
This report involved the developr.ent of a Manual for hazardous material spills
control. This manual is intended for use by people in charge of a spill
clean-up operation or their designated representative, and is not limited
to EPA or U.S. Coast Guard on-scene coordinators. Prior familiarization with
the contents is critical for effective use of the procedures outlined. Since
development equipment is often unavailable for immediate use at a spill site,
emphasis has been placed on using improvised systems to treat hazardous
materials. However, it is stressed that the procedures presented have not
been field tested, and that any improvised system is inherently unsafe.
Therefore, extreme care must be taken to follow all safety precautions and
additional instruction in dealing with hazardous material spills through
training courses, is desired.
This Manual has emphasized spill control, although it is recognized that
prevention techniques are critical and a brief overview of these methods is
included. The control section has been subdivided into eight chapters with
paragraph numbering to aid in cross-referencing. Chapter 1 involves notifi-
cation procedures which are established by the location of the manual user.
An inventory of sources which will provide additional chemical information
is included in Chapter 2.
Chapter 3 presents possible identification methods and then relies on CHFUS-
Vol. 3, Hazard Assessment, for establishing human danger potential. Chapter k
presents a thought guiue approach for determining the best spill handling
method for a given situation. In addition, suggested treatment schemes
for 303 hazardous chemicals are included. Necessary safety procedures and
process design, using a limiting factor approach, are presented in Chapter 5.
Chapter 6 includes construction and operation details for the five improvised
treatment processes (filtration, carbon adsorption, ion exchanges, gravity
separation and chemical reaction)- Treatment components and chemical
considerations are included in Chapter 7 and Chapter 8 includes sampling and
record keeping instruction.
This report was submitted in fulfillment of Contract No. 68-03-221** under
sponsorship of the Environmental Protection Agency. The project was
performed by the Environmental Sciences Division of Envirex Inc. This report
covers work begun in June, 1975 and completed in June, 1977.
i v
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CONTENTS
FOREWORD I | j
ABSTRACT 5v
LIST OF FIGURES vli j
LIST OF TABLES xf;
ACKNOWLEDGMENTS xiv
SECTION
I INTRODUCTION j
II CONCLUSIONS 5
Ml RECOMMENDATIONS 8
IV METHODOLOGY FOR SPILL CONTROL JO
CHAPTER 1 - NOTIFICATION ]]
\.1 General ] ]
1.2 Pertinent Federal Regulations II
CHAPTER 2 - INFORMATION SOURCES 24
2.1 Introduction 24
2.2 EPA Oil 6 Hazardous Materials Technical
Assistance Data System 24
2.3 US Coast Guard CHRIS 33
2.4 Interagency Radiological Assistance
Plan 35
2.5 US Coast Guard National Strike Force 36
2.6 US Army Technical Escort Center Chemical
Emergency Response Team 36
2.7 Chemical Transportation Emergency Center 37
2.8 NACA Pesticides Safety Team Network 38
2.9 Transportation Emergency Assistance Plan 39
2.10 Chlorine Emergency Plan 39
2.11 Information Retrieval Systems 40
2.12 National Emergency Equipment Locator
System 40
2.13 National Analysis of Trends for
Emergencies System 41
2.14 Useful Guides and Reference Handbooks 41
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CONTENTS (continued)
SECTION
CHAPTER 3 - IDENTIFICATION AND ASSESSMENT
3.1 General
3.2 Directions for the First Man on Scene
3-3 Directions for the OSC
CHAPTER 4 - DETERMINATION OF THE BEST METHOD FOR
SPILL HANDLING
4.1 General
4.2 Containment of Spilled Materials
4.3 Collection of Spilled Materials
4.4 Decision on Spill Handling
4.5 Handling a Spill by Hauling
4.6 Handling by Dilution and Dispersal
4.7 Handling by Treatment on Site
CHAPTER 5 - SAFETY CONSIDERATION £ PROCESS DESIGN
5.1 General
5.2 Available Equipment Sources
5.3 Safety Precautions
5.4 System Design Criteria
CHAPTER 6 - PROCESS CONSTRUCTION AND OPERATION
6.1 General
6.2 Filtration
6.3 Carbon Adsorption
6.4 Ion Exchange
6.5 Gravity Separation
6.6 Chemical Reaction
CHAPTER 7 - PROCESS COMPONENTS 6 TREATMENT CHEMICALS
7.1 General
7.2 Process Pumps
7.3 Process Tanks
7.4 Process Components and Flow Control
7-5 Chemical Feed Components
7.6 Air Compressors and Blowers
7.7 Selection of Corrosion Resistant
Materials of Construction
7.8 Information on Treatment Chemicals
7.9 Suppliers Information
7-10 Calculation Aids and Definitions
Page
45
45
45
65
93
93
93
108
117
124
125
125
185
185
188
188
195
239
239
239
253
267
281
304
336
336
336
359
373
382
390
390
399
423
427
v i
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CONTENTS (continued)
SECTION Page
CHAPTER 8 - STANDARD OPERATING PROCEDURES DURING CLEANUP 439
8.1 Samp11ng Procedures 439
8.2 Records 445
V METHODOLOGIES FOR SPILL PREVENTION 447
In Plant Prevention 447
Spill Prevention During Transport 455
Safety or Prevention Devices 462
REFERENCES 467
v i i
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LIST OF FIGURES
No. Page
1 Information segment headers in OHM-TADs 30
2 Identification questions for train spills ^7
3 Typical freight bill for rail shipment ^°
k Identification questions for truck spills ^9
5 Typical truck bill of lading accompanying shipment 50
6 Identification questions for bus spills 51
7 Typical bus bill attached to package 52
8 Identification questions for spills from marine vessels 53
9 Identification questions for spills from barges 5n
10 Identification questions for spills from airplanes 55
11 Identification questions for spills from pipelines 55
12 Identification questions for spills from storage tanks 56
13 Typical packaging label 57
14 Estimating stream widths "2
15 Beaufort scale for wind speed estimation 6*»
16 Hazardous materials warning labels 71
17 Hazard assessment computer system (HACS) hazard assessment tree 76
18 Information needs for CG-M6-3 summary 77
19 Rate of chemical discharge from triangular notch-shaped openings °
20 Rate of chemical discharge from rectangular slot-shaped openings 5
21 Chemical discharge from irregularly shaped holes
22 Comparative carbonless vs. time for the three types of openings 7
23 Effects of toxic gases °9
2k Wind effect on hazard zone 9'
25 Use of Chapter 4 9**
26 Containment of spills on land 97
27 Containment of spills heavier than water 9°
VIII
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LIST OF FIGURES (continued)
No. Page
28 Containment of an entire water mass 99
29 Containment of floating spills 102
30 Suppression of air spills 107
31 Establishing the feasibility of spill containment on land 114
32 Establishing the feasibility of containment for heavier than
water spills 11*
33 Establishing the feasibility of containment for soluble spills 115
34 Establishing the feasibility of containment for 1igher than
water spills 115
35 Establishing the feasibility of air spill suppression 116
36 Spill handling thought guide 118
37 Stepwise use of Chapters 4, 5, 6 and 7 187
38 Summary of a safety director's responsibilities 190
39 Limiting factors in system design 196
40 Schematic of carbon column operation 200
*»1 Pump requirements for unit processes 201
42 Equipment requirements by process element 203
43 Questions to establish limiting factors 204
44 Filter area and media requirements 242
45 Amounts of underdrain material required for column systems 244
46 Preferred option and operating modes - filtration 245
47 Construction details for filters 247
48 Fines scoop 249
49 Backwash volumes for column processes 252
50 Required surface area for carbon columns 257
51 Preferred option and operating modes - carbon adsorption 259
52 Carbon column construction details 261
53 Carbon bed preparation by backwash ing for fines removal 264
54 Operating modes for carbon transfer 266
55 Required surface 271
56 Preferred option and operating modes - ion exchange 273
57 Ion exchange column construction details 275
58 Backwash volume for ion exchange 278
IX
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LIST OF FIGURES (continued)
No. Page
59 Operating modes for ion exchange resin transfer 280
60 Example of settling test graphs 286
61 Batch sedimentation tank schematic 300
62 Serrated outlet hose 301
63 Continuous operated swirl tank presettler 303
6k Schematic diagrams of chemical treatment options 318
65 Installation of jet mixer in rapid mix tank 319
66 Construction of a mechanical flocculator 321
67 Blower size as a function of process volume for an
aeration tank 330
68 Aeration header alternative plan view layouts and
schematic of header support 334
69 Examples of typical system sketches showing pump head
relationships 339
70 Equivalent length of pipe fittings and valves 342
71 Friction loss in water piping 347
72 Typical determinations made from friction loss chart 348
73 Calculation information for tank volumes 360
7k ASTM head volumes 363
75 Information needed to obtain suitable chemical feed
equipment 384
76 Data sheet on acetic acid 405
77 Data sheet on aluminum sulfate 406
78 Data sheet on calcium chloride 407
79 Data sheet on calcium hydroxide 408
80 Data sheet on calcium oxide 409
81 Data sheet on ferric chloride 410
82 Data sheet on ferrous sulfate 411
83 Data sheet on hydrochloric acid 412
84 Data sheet on polyelectrolytes 413
85 Data sheet on potassium permanganate 414
86 Data sheet on sodium bicarbonate 415
87 Data sheet on sodium bisulfate 416
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LIST OF FIGURES (continued)
No.
88 Data sheet on sodium carbonate 417
89 Data sheet on sodium hydroxide 418
90 Data sheet on sodium hypochlorlte 419
91 Data sheet on sodium sulfate 420
92 Data sheet on sodium sulfide 421
93 Data sheet on sulfuric acid 422
gli Format for chemical suppliers information 428
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LiST OF TABLES
No. Page
1 INITIAL NOTIFICATION FOR HAZARDOUS MATERIAL SPILLS 12
2 EPA REGIONAL OFFICES 13
3 US COAST GUARD DISTRICTS \k
k CANADIAN ENVIRONMENTAL PROTECTION SERVICE CONTACT LIST 15
5 APPROPRIATE STATE AGENCIES TO CONTACT 17
6 LIST OF INFORMATION SYSTEMS 25
7 INFORMATION RETRIEVAL SYSTEMS 29
8 REFERENCES TO USE IN CONJUNCTION WITH THIS MANUAL *»2
9 METHODS OF IDENTIFYING SPILL LOCATION 60
10 COMPATIBILITY CHART TAKEN FROM CHRIS CG U6-I 67
11 SUMMARY OF HOW TO OBTAIN SHIPPING PAPER COPIES 69
12 HAZARDOUS CHEMICALS DESIGNATED BY THE COAST GUARD 73
13 CALCULATIONS AVAILABLE IN CHRIS HAZARD ASSESSMENT 75
14 USABLE VOLUME OF SHIPPING CONTAINERS 78
15 TYPICAL CARRIER CAPACITIES 81
16 OIL CONTAINMENT REFERENCES 96
17 SPILLS ON LAND 109
18 SPILLS IN WATER - HEAVIER THAN WATER SPILLS 110
19 SPILLS IN WATER - SOLUBLE OR MISCIBLE SPILLS 111
20 SPILLS IN WATER - FLOATING SPILLS 112
21 SPILLS IN AIR 113
22 POSSIBLE TREATMENT SCHEMES 132
23 EQUIPMENT SOURCES 189
2k MANPOWER REQUIREMENTS FOR VARIOUS UNIT PROCESSES PER SHIFT 198
25 COLUMN OPERATION DISCHARGE LINE SIZING 2^8
26 DESIGN PARAMETERS USED FOR ION EXCHANGE 269
27 TREATMENT CHEMICAL INFORMATION 292
x i i
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LIST OF TABLES (continued)
No. Page
28 CHEMICAL REACTION OPERATING PARAMETERS 30?
29 FLUID PUMPING TERMS 3*0
30 PRELIMINARY LINE SIZING CHART
31 FORM FOR CALCULATION OF TOTAL DYNAMIC HEAD AND TOTAL
SUCTION LIFT
3*3
31a COMPLETED FORM FOR CALCULATION OF TOTAL DYNAMIC HEAD AND
TOTAL SUCTION LIFT 350
32 PUMP SELECTION CHART 35*
33 TYPICAL RATING FOR MEDIUM PRESSURE CENTRIFUGAL PUMPS 353
34 TYPICAL AIR PUMP SPECIFICATIONS 357
35 SYNTHETIC LINER MATERIALS 36?
36 INFORMATION ON CORROGATED STEEL 369
37 REINFORCED CONCRETE PIPE INFORMATION 370
38 SOIL STRENGTH AND DENSITY INDICATORS 371
39 COMMERCIALLY AVAILABLE HOSES 37*
*0 MATERIALS OF CONSTRUCTION FOR TYPE A PUMPS 386
*1 MATERIALS OF CONSTRUCTION FOR POSITIVE DISPLACEMENT PUMPS 387
*2 TYPICAL THERMOPLASTIC TUBE SIZE 389
*3 SOURCES AND SIZES OF AIR COMPRESSORS 391
*4 PROPERTY COMPARISONS - NATURAL AND SYNTHETIC RUBBERS 396
*5 PROPERTIES OF COMMERCIALLY AVAILABLE PLASTICS 397
xiii
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ACKNOWLEDGMENTS
The authors gratefully acknowledge the assistance from many individuals and
organizations in the preparation of this document. Special thanks are
extended to the staff of the Oil and Hazardous Material Spills Branch of
the Industrial Environmental Research Laboratories in Edison, New Jersey.
In particular, the direction and support of Mr. Ira Wilder, Branch Chief and
Project Officer, is especially appreciated. In addition, helpful advice
from Mr. Frank Freestone, Dr. Joseph LaFornara and Dr. John Brugger is
acknowledged.
Input from Coast Guard officials, various strike teams and EPA on-scene
coordinators was also appreciated during the preparation of this Manual,
since their experience provided vital background information. Finally,
thanks are extended to the entire staff of the Environmental Sciences
Division—technical, clerical and administrative—who participated in this
project and contributed to its success.
X I V
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SECTION I
INTRODUCTION
Increased concern over and regulations concerning the spills of hazardous
materials into the environment, along with increasing use of toxic chemicals,
have resulted in a growing necessity for treating spills. A spill situation
requires immediate response for containment and then treatment of the con-
taminated media. However, only a limited supply of existing equipment is
available for hazardous spill control. Therefore, this Manual was developed
to present possible improvised treatment processes for hazardous spill miti-
gation. In addition, general information required by those using this
Manual, including notification procedures, additional information sources,
and identification and assessment techniques, are included. Suggested
treatment processes for each of the 303 hazardous chemicals are included,
but it must be emphasized that they have not been field tested.
This Manual is intended for use by people in charge of a spill cleanup
operation and/or their designated representative at the scene of the spill.
it is not limited to use by EPA or US Coast Guard on-scene coordinators, but
is applicable to various industry personnel or others dealing with hazardous
chemicals. The main requirement for effective use of this Manual is to
understand the basis for its development and be familiar with the contents
prior to a spill occurrence. It is also desirable to have additional in-
struction in dealing with hazardous chemical spills through training courses
such as those offered by National Fire Protection Association (NFPA) or
Vanderbilt University. Finally, the Manual should be used in conjunction
with many other references that must be readily available to the user.
Prior to the detailed use of this Manual, several important factors must be
considered. The first factor is that the improvised treatment processes as
proposed are presented as a last resort method for treatment. More sophis-
ticated and, therefore, safer equipment might be available and should be
used, if possible. Another consideration is that the proposed equipment
designs are just one alternative approach to the development of the unit
processes. Imaginative spill control coordinators can modify the design de-
pending upon available materials, site restrictions, etc. It must also be
re-emphasized that these methods and the treatment schemes have not been
field tested. Interfering factors at a spill site may affect the treatment
in an adverse manner and a spill control coordinator must be aware of these
possible problems. Strict enforcement of safety procedures is mandatory
for safe spill control. Also, an appointed safety director must be aware
of potential safety hazards and inform personnel of the risks Involved.
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Due to the complexity of potential spill events, this Manual has presented
a generalized approach to spill control. Each of the 303 hazardous chemicals
have been considered separately when the suggested treatment schemes were
developed. Mixtures must be handled with care by consulting references and
manufacturing experts who can indicate possible chemical by-products. The
treatment schemes presented in this Manual are basically concentration
processes. The residuals of treatment, including sludges and spent media,
must be disposed of properly. However, this Manual does not attempt to
address the complicated problems of disposal.
This Manual considers both spill control and spill prevention. The emphasis
has been on spill control. A summary section which considers spill pre-
vention techniques is included. Further reference to other documents deal-
ing with spill prevention is recommended. Section IV, entitled "Methodology
for Spill Control" contains the major emphasis for on-site spill handling.
It has been divided into chapters with subdivision numbering for cross-
references. The eight chapters deal with different, but related aspects of
spill control. Reference to specialized documents in certain areas has been
included and it will be necessary for the spill coordinator to have this
additional information readily available. Also, there are certain sections
of this Manual which require major input by the spill control coordinator
who may use this Manual. This is the situation when considering local
spill notification requirements, and identifying local suppliers of equip-
ments and auxiliary chemicals.
The following chapters are included:
Chapter 1: Notification
This chapter briefly discusses the legal requirements for notification.
However, it requires some preparatory work by the user since individual
notification requirements vary by locality. The local government and
appropriate state agency must be contacted to determine actual notification
requirements, and lists of these agencies are included.
Chapter 2: Information Sources
This chapter provides a brief inventory of various information sources that
are available to aid in the event of a spill situation. The sources have
not been evaluated but have only been listed with their information capa-
bilities and access telephone numbers.
Chapter 3: Identification and Assessment
In this chapter, various steps to allow identification of the chemical
spilled and then to assess the human danger potential are included. It is
emphasized that only an on-scene coordinator or a designated representative
should follow the procedures and then only if the appropriate safety pre-
cautions are taken. If the identity of a spill is completely unknown, it
is not recommended that the spill be approached. The assessment portion of
the chapter relies heavily on reference to CHRIS Volume 3 "Hazard Assessment",
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since duplication of the information presented there was not desirable. Sug-
gestions for collecting needed information at the spill site are included
for field use.
Chapter A: Determination of the Best Method for Spill Handling
Chapter k presents a brief overview of containment methods and relies on oil
spill control references to provide the needed details. The next portion
of the chapter includes a thought guide model which allows determination of
the best method for handling a spill given various considerations.
Once this decision is reached, the various handling methods are discussed
with emphasis on off-stream but on-site treatment methods. Suggested
methods of treating the 303 hazardous chemicals are included, but none of
the methods have been field tested. They were developed based on industrial
wastewater treatment methods, when available, chemical properties and the
knowledge of experienced personnel. References are included to allow
further research.
Chapter 5: Safety Precautions and System Design
Once it has been established from Chapter k that treatment off-stream but
on-site is desirable, then the system must be designed. Chapter 5 first
lists other equipment sources that should be used if available. If it is
necessary to jury-rig a treatment process, strict safety procedures outlined
in this chapter should be followed. Finally, in order to design the most
effective system prior to construction, a limiting factor approach is de-
sirable. In this procedure, several different variables are considered and
the limiting design flow rate is established. Three examples illustrate
the technique.
Chapter 6: Process Construction and Operation
This chapter provides description of each of the five unit processes plus
detailed instructions regarding performance of appropriate bench tests.
Their individual design and construction steps are included. Finally,
operation and troubleshooting directions are included for use in the actual
treatment.
Chapter 7' Process Components and Treatment Chemicals
A wide variety of critical information is included in this chapter regarding
the individual components of the treatment train. Information given includes
tank and pump sizing and selection, hoses and fitting specification, and
materials of construction. Treatment chemical information includes data
sheets providing pertinent properties and a partial list of suppliers. It
is recommended that the user of this Manual list potential suppliers of
all treatment chemicals and other equipment before a spill occurrence.
Chapter 8: Standard Operating Procedure During Clean-Up
Information regarding sampling and record keeping procedures to be used dur-
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ing the clean-up operation are included. Both composite and grab samples
are discussed along with the mechanics of collection and appropriate sample
locations. Sample bottle preparation, sample identification and chain of
custody procedures are also presented. Record keeping involves a detailed
notation of the field occurrences. Several important records are presented.
This Manual provides a broad range of information for the spill coordinator.
But it must be re-emphasized that none of the procedures, with the possible
exception of safety precautions are mandatory. The various situations
which occur at a spill site cannot be anticipated, so that the procedures
presented in this Manual must be applied with caution. The dangers associ-
ated in handling a spilled hazardous material cannot be underestimated, so
it is strongly recommended that safety be the first priority of those on
the scene of a spi11.
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SECTION I I
CONCLUSIONS
GENERAL
In order for this Manual to be effective, it is essential that its potential
users be thoroughly familiar with its contents and method of use prior to an
actual spill situation.
This Manual contains the minimum requi red information for treating hazardous
spills in improvised field situations. It is necessary to have available for
immediate use other, more detailed, references specified in this text.
In addition to this Manual, training courses are available to aid personnel
in charge of Hazardous Materials spill control. Among the courses offered
are a week-long program through Vanderbilt University, a National Fire Pro-
tection Association course on control of accidental releases of hazardous
chemicals, and others.
SAFETY AND HAZARD ASSESSMENT
The control of hazardous materials spills presents inherently unsafe condi-
tions for personnel and these problems are compounded when improvised equip-
ment is utilized. Therefore, the suggested procedures included in this
Manual should be used only when other equipment is not available. Extreme
caution is necessary when performing any task and prior awareness of the
risks involved is essential. If the identity of the materials spilled is
unknown, the safety hazards cannot be defined. Therefore, the spill should
not be approached, without a complete protective enclosure or suit offering
maximum isolation from the "worst case" spilled material.
This Manual presents only the basic requirements for one method of field
implementation of the suggested treatment processes. It is anticipated that
in many field situations, even these requirements cannot be met. Therefore,
this Manual is not intended to replace well-trained quick thinking personnel
in charge of spill control, but rather it is to serve as an aid and primary
reference for their use.
Each person likely to be confronted with a spill should determine the proper
reporting procedure before any actual spill occurs. In addition to the
requirements of National and Regional Contingency Plans, the state reporting
requirements must also be met. According to U.S. Coast Guard Regulation,
spills of hazardous substances that may affect water sources should be
reported to the National Spill Response Center, 800-42^-8802.
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Information sources presented in this document have not been evaluated, but
rather have been included to provide a broad base of additional needed input.
Identification of a hazardous spill material can be accomplished and verified
by the following methods: examination of shipping papers, recognition of
physical properties, analysis for chemical properties, or confirmation with
the manufacturer or shipper.
Information needed for proper assessment of the hazard potential of a spill
should be collected by the spill control coordinator or a designated repre-
sentative (defined in this Manual as the Man on the Scene (MOS) and relayed
to others for further analysis, if needed.
RESPONSE DECISION ANALYSIS
Immediate remedial action, including proper containment methods, is specific
to each spill situation. Instructions for implementing remedial action can
only be issued after the spill has been identified and assessed.
There are three basic methods available for handling a hazardous spill. The
methods are 1) collecting and hauling the material to a remote location,
2) in-situ treatment of the contaminated media, and 3) treatment in an off-
stream but on-site treatment system. As a means of last resort, dilution and
dispersal may have to be used to minimize the local impact of a concentrated
spill.
Determining the best method of handling a spill requires the evaluation of
many variables which affect the situation and will ultimately lead to a
logical solution.
Although improvised treatment schemes have been suggested for the 303 chem-
icals designated as hazardous by the U.S. Environmental Protection Agency,
many factors, including personnel safety, may dictate on-site treatment to be
the least feasible of all available alternatives.
A "limiting factors design" approach has been developed to allow a determi-
nation of those variables that control the rate (and thus the time required)
at which the hazardous spill may be treated.
Generally, on-site or in-situ treatment (as opposed to hauling or pumping to
a remote location) is the best method of spill cleanup only when the haz-
ardous material has entered a body of water or has been highly diluted by
some other means.
WATER TREATMENT METHODS
It was found that five basic unit processes would be sufficient for the com-
bination of treatment processes required for treating most of the 303 mate-
rials of concern. These processes are 1) filtration, 2) carbon adsorption,
3) ion exchange, k) gravity separation, and 5) chemical reaction (oxidation/
reduction, neutralization, and precipitation).
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Batch processes are necessary in improvised treatment systems for many pro-
cesses because of the unavailability of sophisticated instrumentation for
synchronization. However, by constructing a number of batch processes in
parallel, a near continuous mode of operation can be achieved.
The use of equalization tanks between individual unit processes simplifies
the operation and interconnection logistics between batch processes (e.g.,
gravity separation and chemical treatment) and continuous flow-through pro-
cesses (e.g., filtration, carbon adsorption and ion exchange).
Design procedures are outlined for sizing holding tanks for the effluent from
the treatment process until analytical results are available. However, the
turnover time of the analytical tests, if not performed on site, may require
the implementation of an unreasonably large number of storage tanks.
The suggested materials for construction of the treatment processes are those
that are readily available from many sources. However, in cases where the
easily accessible materials cannot accomplish a task safely (e.g., pumping of
corrosive treatment materials), it was necessary to specify special equipment,
The suggested treatment process chemicals have been limited to those that are
readily available from chemical supply houses.
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SECTION IN
RECOMMENDATIONS
I. Identification of people in a given geographical area with expertise in
control of hazardous materials should be made and then listed with phone
numbers for immediate reference. Also, sources of reliable supplies of
common materials and equipment used for spill cleanup should be listed
and continually updated.
2. Central storage locations should be developed where common equipment
items such as chemicals, tanks, booms, carbon, filter media, etc., can
be stored in inventory so that these materials will be readily available
on a payback basis when a spill occurs.
3. This Manual should ultimately be divided into two separate parts. The
first part would contain the appropriate chapters on notification, spill
identification, and assessment. This document would have very broad
distribution, including local fire departments, etc. The second part,
that would contain extensive information on spill treatment, would
have a much smaller distribution.
L\, The number of hazardous materials covered in this Manual should be in-
creased to include all those presently listed in OHM-TADS and CHRIS.
5. The treatment schemes suggested in this Manual were based on the existing
literature coupled with the contractor's experience in this field.
Although the treatment schemes are considered to be applicable, many
of these schemes should be field tested. These tests would uncover
any obvious shortcomings in design or approach, safety hazards and
possible problem areas and would allow recommendation for improved con-
struction and treatment procedures.
6. Since bench scale treatability studies are an integral part of using this
Manual, persons intending to use them should be trained in these
techniques. Also, bench scale test kits containing the required chemicals
and equipment should be assembled and available in each central hazardous
spill response location.
7- A research study should be performed to develop simple tests for quantita-
tive and rapid analysis of toxic and hazardous materials. These tests
must be applicable for on-site use with a minimum of sophisticated
equipment.
-------
8. All sources providing information with regard to the potential safety
hazards of a spilled material should devise a common reporting format
of input for use by on-site personnel.
-------
SECTION IV
METHODOLOGY FOR SPILL CONTROL
This section of the report contains the main thrust of the manual itself.
The techniques to control spills have been presented using a numbered
chapter format for ease of cross-reference. The section has been divided
into 8 chapters as follows:
Chapter 1: Notification
Chapter 2: Information Sources
Chapter 3: Identification and Assessment
Chapter ^: Determination of the Best Method for Spill Handling
Chapter 5: Safety Considerations and Process Design
Chapter 6: Process Construction and Operation
Chapter 7- Process Components and Treatment Chemicals
Chapter 8: Standard Operating Procedure During Clean-up
As previously stated, it is important for the user of this Manual to be
familiar with the content and have previously completed certain informa-
tion sections. The chapters have been presented in the basic order in
which they will be most useful, however, it will be necessary to refer
to other chapters, especially during the process design. Therefore over-
all familiarity with the manual is critical for its most effective use.
10
-------
1.0 CHAPTER I - NOTIFICATION
I.I GENERAL
The objective of this chapter is to assist and encourage the user of this
manual to determine the proper initial notification procedure for the
immediate reporting of a hazardous material spill in his area. This pro-
cedure should be determined before any actual spill occurs. It is in-
tended that each user enter the proper contacts and telephone numbers in
Table I as he finds appropriate. In this regard the National, State, and
Regional Contingency Plans should serve as reference documents and should be
kept with this manual. It should be pointed out that all reporting require-
ments must be met and that State reporting requirements are often more encom-
passing than Federal requirements. For example, a spill on land only may be
covered by State but not by Federal regulation. Also, this discussion covers
initial and immediate reporting only; there may also be requirements for
later detailed reports to the Regional or State Response Centers and the
U.S. Department of Transportation.
It is the responsibility of the user of this Manual to be aware of the re-
gional reporting requirements. To aid in this determination, Tables 2-5
have been included. These tables include the appropriate State and Federal
agencies to be contacted in various areas. Telephone numbers have been in-
cluded where possible although they change periodically; the appropriate
agencies should be contacted to determine their current reporting numbers.
The needed information regarding notification requirements should be trans-
ferred to Table 1 for future reference.
1.2 PERTINENT FEDERAL REGULATIONS
The National Oil and Hazardous Substances Pollution Contingency Plan was
developed in compliance with the Federal Water Pollution Control Act (Public
Law 92-500). The Plan provides for a pattern of coordinated and integrated
response by Departments and Agencies of the Federal Government to protect
the environment from the damaging effects of pollution discharges. The Plan
as published in the Fed e raj Register, Vol. 40, No. 28- outlines the notifica-
tion requirements. In this regard Annex V of the Plan states:
"1503-2 The initial reporting of a pollution discharge by
agencies participating in this plan shall be in accordance with
the information and format as described in the regional plans.
Reports of medium or major discharge received from discharges
or the general public by the National Response Center (NRC) shall
be relayed by telephone to predesignated On-Scene Coordinator (OSC)."
The Plan also specified the National Response Center, located at Head-
quarters, U.S. Coast Guard, Washington, D.C., as the headquarters site for
activities relative to pollution emergencies. The National Response Team,
consisting of representatives from various Federal agencies, serves planning
and response functions and is to work closely with the National Response
Center.
11
-------
TABLE 1. INITIAL NOTIFICATION PROCEDURE FOR HAZARDOUS
MATERIAL SPILLS (to be completed by user)
Agency Comments
1. Name: National Response Center
Address: Headquarters, U.S. Coast Guard
Washington, D.C.
Contact: NRC Duty Officer
Tel. No.: 800/^-8802 (24-hr)
2. Name: U.S. EPA Regional Office
Region No.
Address :
Contact: ^ ^
Tel. No.: (day)
(night)
3. Name: U.S. Coast Guard District Office
District No.
Address:
Contact:
Tel. No.: ~ (dayT
(night)
State Agency:
Address:
Contact:
Tel. No.: ~~ (day)
(night)
5. For spill on or near international waters
Foreign Govt. Agency:
Address:
Contact:
Tel. No.: (day)'
(night)
12
-------
TABLE 2. EPA REGIONAL OFFICES
I. Environmental Protection Agency
Region I , Room 2303
John F. Kennedy Federal Building
Boston, Massachusetts 02203
Tel: (617) 223-7265
II. Environmental Protection Agency
Regional I I, Room 908
26 Federal Plaza
New York, New York 10007
Tel: (201) 548-8730
III. Environmental Protection Agency
Reg i on III
Curtis Bldg.
6th and Walnut Streets
Philadelphia, Pennsylvania 19106
Tel: (215) 597-98g8
IV. Environmental Protection Agency
Region IV
1421 Peachtree St., N.E.
Atlanta, Georgia 30309
Tel: (404) 526-5062
V. Environmental Protection Agency
Region V
230 South Dearborn Street
Chicago, Illinois 60604
Tel: (312) 896-7591
VI. Environmental Protection Agency
Region VI, Suite 1600
1600 Patterson St.
Dal las, Texas 75201
Tel: (214) 749~3840
VII. Environmental Protection Agency
Reg i on VII
1735 Baltimore Ave.
Kansas City, Missouri 64108
Tel: (816) 374-3778
VIII. Environmental Protection Agency
Region VIII, Suite 900
i860 Lincoln Street
Denver, Colorado 80203
Tel: (303) 837-3880
IX. Environmental Protection Agency
Region IX
100 California Street
San Francisco, California 94111
Tel: (415) 556-6254
X. Environmental Protection Agency
Region X
1200 Sixth Avenue
Seattle, Washington 98101
Tel: (206) 442-4343
States Included
Maine, Vermont, New Hampshire,
Massachusetts, Rhode Island and
Connecticut
New York, New Jersey and Puerto Rico
Pennsylvania, Maryland, Delaware,
West Virginia and Virginia
Kentucky, Tennessee, North Carolina,
South Carolina, Georgia, Alabama,
Mississippi and Florida
Ohio, Michigan, Indiana, Illinois
Wisconsin and Minnesota
Arkansas, Louisiana, Oklahoma,
Texas and New Mexico
Iowa, Missouri, Nebraska and
Kansas
North Dakota, South Dakota,
Montana, Wyoming, Utah and
Colorado
Nevada, Arizona, California,
Hawai i and Guam
Idaho, Oregon, Washington and
Alaska
13
-------
TABLE 3. U.S. COAST GUARD DISTRICTS
UNITED STATES DEPARTMENT OF TRANSPORTATION
U. S. COAST GUARD DISTRICTS
•14
1st Coast Guard District
150 Causeway Street
Boston, Mass. 02114
Duty Officer: (617) 223-6650
2nd Coast Guard District
Federal Building
1520 Market Street
St. Louis, Mo. 63101
Duty Officer: (314) 622-4614
3rd Coast Guard District
Governors Island
New York, N.Y. 1000*1
Duty Officer: (212) 264-4800
5th Coast Guard District
Federal Building
431 Crawford Street
Portsmouth, Va. 23705
Duty Officer: (703) 393-9611
7th Coast Guard District
Room 1018, Federal Bldg.
51 S.W. 1st Avenue
Miami , Fla. 33130
Duty Officer: (305) 350-5611
8th Coast Guard District
Customhouse
New Orleans, La. 7013C
Duty Officer: (504) 527-6225
9th Coast Guard District
1240 East 9th Street
Cleveland, Ohio 44199
Duty Officer: (216) 522-3984
11th Coast Guard District
Heartwell Bldg.
19 Pine Avenue
Long Beach, Calif. 90802
Duty Officer: (213) 590-2311
12th Coast Guard District
630 Sansome Street
San Francisco, Calif. 94126
Duty Officer: (415) 556-5500
13th Coast Guard District
618 2nd Avenue
Seattle, Washington 95104
Duty Officer: (206) 524-2902
14th Coast Guard District
677 Ala Moana Blvd.
Honolulu, Hawaii 96813
Duty Officer: (808) 546-7109
(Commercial Only)
AUTOVON 421-4845
17th Coast Guard District
P.O. Box 3-5000
Juneau, Alaska 99801
Duty Officer: (907) 586-7340
(Commercial Only)
AUTOVON 388-1121
-------
TABLE k. CANADIAN ENVIRONMENTAL PROTECTION SERVICE EMERGENCY CONTACT LIST
ATLANTIC REGION
Halifax
RD: Dr. C. J. Edmonds
P.O. Box 2**06
Halifax, N.S.
EEC: Mr. H. T. Doane
P.O. Box 2A06
Halifax, N.S.
Newfoundland
DM: Mr. I. G. Sherbin
Building 310
Pleasantvl 1 le
St. John's,
Newfoundland A1A 2Y3
NATIONAL HEADQUARTERS
Ottawa
National Manager:
Mr. R. A. Beach
15th Floor
Place Vincent Massey
Ottawa, Ontario
K1A OH3
Assistant Manager
National Environmental
Emergency Centre:
15th Floor
Place Vincent Massey
Ottawa, Ontario
KIA OH3
QUEBEC REGION
Montreal Toronto
RD: Mr. G. M. Gauthler RD:
P.O. Box 1330
Station B
Montreal 110, Quebec
Dr. R. W. Slater
135 St. Clair Ave. , H
Toronto, Ontario
IPS
EEC: Mr. Y. Plunier EEC:
P.O. Box 1330
Station B
Montreal 110, Quebec
Mr. N. Vanderkooy
135 St. Clair Ave. , W
Toronto, Ontario
1P5
Ottawa
National Capital Area Manager:
Mr. L. J, Kamp
^5 Spancer St.
Ottawa, Ontario
K1Y 2P5
cont inued
NOTE: RD: Regional Director
EEC: Environmental Emergency Coordinator DM: District Manager
-------
TABLE 1» (continued)
NORTHWEST REGION
Edmonton
RD: Mr. J, J. Eatock
10th Floor
Imperial Oil Building
10025 Jasper Ave.
Edmonton, Alberta
T5J 2X9
EEC: Mr. R, K. Pettigrew
10th Floor
Imperial Oil Building
1005 Jasper Ave.
Edmonton, Alberta
T5J 2X9
Wlnnlpeg
DM: Mr. H. C. R. Gavin
9th Floor
303 Main St.
Winnipeg, Malntoba
R3C 3G7
Ye 11owkn i fe
DM: Mr. W. J. Bryant
9th Floor
Bellanca Bldg.
YellowV.nife, N.W.T.
Vancouver
D-0: Mr. R. E, McLaren
Kap?lano 100
Park Royal
Vancouver, B.C.
V7T 1A2
Whttehorse
DM: Mr. C. E. Wykes
Room 102
Mainsteele BuiIding
212 Main St.
Whitehorse, Y,T.
VIA 2B1
-------
TABLE 5. APPROPRIATE STATE AGENCIES TO CONTACT
ALASKA
Oept. of Environmental
Pouch 0
Juneau, AK 99801
Conservation
ALABAMA
Alabama Water Improvement Commission
State Office Bldg.
Montgomery, AL 36104
ARIZONA
State Department of Health Services
Environmental Health Services Division
Bureau of Water Quality Control
17^0 W. Adams
Phoenix, AZ 85007
ARKANSAS
Department of Pollution Control and Ecology
Water Division
8001 National Drive
Little Rock, AR 72209
CALIFORNIA
State Water Resources Control Board
Legal & Enforcement Section
P.O. Box 100
Sacramento, CA 95801
COLORADO
Colorado Dept. of Health
Water Quality Control Division
4210 E. llth Avenue
Denver, CO 80220
CONNECTICUT
Department of Environmental Protection
165 Capitol Avenue
Hartford, CT 06115
DELAWARE
Department of Natural Resources
Division of Environmental Control
Tatnall Building
Dover, DE 19901
FLORIDA
Department of Environmental Regulation
2562 Executive Center Circle East
Montgomery Building
Tallahasee, FL 32301
continued
-------
TABLE 5. (continued)
GEORGIA
Department of Natural Resources
Environmental Protection Division
270 Washington Street, S.W.
Atlanta, GA 3033^
HAWAII
Environmental Protection £ Health Services Division
P.O. Box 3378
Honolulu, HI 96801
IDAHO
Dept. of Health 6 Welfare
Division of Environment
Statehouse
Boise, ID 83720
ILLINOIS
Environmental Protection Agency
2200 Churchil1 Road
Springfield, IL 62706
INDIANA
IOWA
Indiana Stream Pollution Control Board
1330 West Michigan Street
Indianapolis, IN 46206
Iowa Water Quality Commission
Department of Environmental Quality
P.O. Box 3326
Des Moines, IA 50319
KANSAS
State Department of Health £ Environment
Division of Environment
Topeka, KS 66620
KENTUCKY
Department for Natural
and Environmental
Division of Water
Capitol Plaza Tower
Frankfort, KY 40601
Resources
Protection
LOUISIANA
Louisiana Stream Control Commission
P.O. Drawer FC
University Station
Baton Rouge, LA 70803
continued
-------
TABLE 5 (continued)
MAINE
Maine Department of Environmental Protection
State House
Augusta, ME 04330
MARYLAND
Water Resources Administration
Tawes State Office Building
Annapol is, MD 21401
MASSACHUSETTS
Division of Water Pollution Control
100 Cambridge St.
Boston, MA 02202
MICHI CAN
Dept. of Natural Resources
Water Quality Commission
84 Mason Bldg.
Lansing, Ml 48926
MINNESOTA
Minnesota Pollution Control
1935 W. County Rd. B2
Roseville, MN 55113
Agency
MISSISSIPPI
Mississippi Air 6 Water Pollution
Control Commission
P.O. Box 827
Jackson, MS 39205
MISSOURI
Department of Natural Resources
Division of Environmental Quality
Water Quality Program
P.O. Box 1368
Jefferson City, MO 65101
MONTANA
Dept. of Health 6 Environmental Sciences
Water Quality Bureau
Cogswe11 BuiIdi ng
Helena, MT 59601
NEVADA
NEW HAMPSHIRE
State Environmental Commission
102 Johnson St.
Carson City, NV 89701
New Hampshire Water Supply & Pollution
Control Commission
105 Loudon Rd.
Concord, NH 03301
continued
19
-------
TABLE 5 (continued)
NEW JERSEY
N.J. Dept. of Environmental Protection
Division of Water Resources
P.O. Box 2809
Trenton, NJ 08625
NEW MEXICO
Environmental
Water Quality
P.O. Box 2348
Santa Fe, NM 87503
Improvement Agency
Division
NEW YORK
State Dept. of Environmental Conservation
Bureau of Monitoring & Surveillance
50 Wolf Road, Rm 306
Albany, NY 12201
NORTH CAROLINA
Dept. of Natural 6 Economic Resources
Division of Environmental Management
P.O. Box 2768?
Raleigh, NC 27611
NORTH DAKOTA
State Dept. of Health
Division of Environmental Engineering
State Capital BuiIding
Bismarck, NO 58501
OHIO
Ohio Environmental
P.O. Box 1049
Columbus, OH 43216
Protection Agency
OKLAHOMA
State Dept. of Health
Occupational & Radiological Health Service
P.O. Box 53551
Oklahoma City, OK 73105
OREGON
State Department of Environmental Quality
123^ S.W. Morrison
Portland, OR 97205
PENNSYLVANIA
Dept. of Environmental Resources
Bureau of Water Quality Management
P.O. Box 2063
Harrisburg, PA 17120
continued
20
-------
TABLE 5. (continued)
PUERTO RICO
Environmental Quality Board
San Juan, Puerto Rico 00910
RHODE ISLAND
Rhode Island Dept. of Health
Division of Water Supply 6 Pollution Control
209 Health Building
Davis Street
Providence, Rl 02908
SOUTH CAROLINA
Office of Environmental
Monitoring Division
J. Marion Sims Building
2600 Bull St.
Columbia, SC 29201
Quality Control
SOUTH DAKOTA
Dept. of Environmental Protection
Joe Foss BuiIding
Pierre, SD 57501
TENNESSEE
Tennessee Division of Water Quality Control
621 Cordell Hull Building
Nashville, TN 37219
TEXAS
Water Quality Control Board
P.O. Box 132J»6, Capital Station
Austin, TX 78711
UTAH
State Division of Health
Bureau of Water Quality
kk Medical Drive
Salt Lake City, UT
VERMONT
Agency of Environmental Conservation
Water Quality Division
State Office Bldg.
Montpelier, VT 05602
VIRGINIA
State Water Control Board
Bureau of Surveillance & Field Studies
P.O. Box 11 H»3
Richmond, VA 23219
continued
21
-------
TABLE 5. (continued)
VIRGIN ISLANDS
Health Department
St. Thomas, Virgin Islands 00801
WASHINGTON
WISCONSIN
State Dept. of Ecology
Olympia, WA 98504
Department of Natural Resources
Bureau of Water Quality
P.O. Box 450
Madison, Wl 53701
WEST VIRGINIA
Dept. of Natural Resources
Division of Water Resources
1201 Greenbrier St.
Charleston, WV 25311
WYOMING
Dept. of Environmental Qual
Water Quality Division
State Office Building West
Cheyenne, WY 82002
ty
22
-------
The Plan also provides for Regional Response Centers and Regional Response
Teams. The Regional Response Center is the regional site for pollution
emergency response activities. Each region has prepared a contingency plan
to deal with oil and hazardous material spills in its region. The Re-
gional Response Team performs response and advisory functions in its speci-
fic region.
The user of this Manual should obtain a copy of the contingency plan for his
region if he does not have one. The regional contingency plan contains de-
tailed information on the response center location, telephone numbers of the
appropriate agencies to contact, and geographic boundaries for the various
agencies.
23
-------
2.0 CHAPTER 2 - INFORMATION SOURCES
2.1 GENERAL
There are a number of information systems whose main function is to provide
assistance during hazardous materials spills. These systems are listed in
Table 6. There are also information retrieval services - both computerized
and manual - which provide information or a list of titles or abstracts of
articles dealing with a specific subject. The organizations which provide
these services are listed in Table 7. The availability of an on-line com-
puter usually indicates a short turn-around time for responses. This is
often important in an emergency situation. There are also available numer-
ous reference texts and handbooks which contain information on the proper-
ties of hazardous chemicals. Those likely to be faced with a hazardous
material spill may find it helpful to obtain one or more of these books for
future reference. Several useful handbooks are listed in this section.
Each system designed specifically to provide information on hazardous
materials is discussed in terms of what it is, what information it contains,
how it operates, and how it can be accessed by responsible people at the
emergency scene. The manual does not attempt to provide an evaluation of
these information sources, but rather it is only an inventory with perti-
nent information required for use.
2.2 EPA OIL AND HAZARDOUS MATERIALS TECHNICAL ASSISTANCE DATA SYSTEM
(OHM-TADS)
2.2.1 Description
The OHM-TADS is a computerized information retrieval file on more than 850
oil and hazardous substances. The system is presently on-line and available
to assist in identification of a spilled material from certain observations
(color, smell, etc.) made at the site. For each substance there are 123 in-
formation segments (see Figure 1) covering a wide variety of physical, chemi-
cal, biological, toxicological, and commercial data with the greatest empha-
sis on the effects on water quality. Of the 123 segment headers 95 can be
used as search components.
2.2.2 Mode of Operation
The OHM-TADS has a random access provision which enables the user to solve
problems involving unidentified pollutants by inputting color, odor or other
physical/chemical characteristics as observed on-scene. The system auto-
matically takes each word and processes it into an inverted index file,
making each word a search component of the data base. The search is made
using Boolean logic and the system responds with a list of the materials
meeting the input characteristics. The output is displayed on the user's
terminal. The user can then refine the search if necessary to narrow the
list of possible materials.
In looking for characteristics of the spill to aid in identification, the 95
searchable headers should be examined to see if any of them can serve as
ident i fiers.
2k
-------
TABLE 6. SOURCES OF INFORMATION/ASSISTANCE FOR HAZARDOUS MATERIAL SPILLS
Information source
EPA Oi 1 and Hazardous
Type of
Organization
Federal
Type of
Informat ion
Assistance3
2-A
Access
EPA Regional Office
Materials - Technical
Assistance Data System
(OHMTADS)
Coast Guard Chemical
Hazards Response
Information System
(CHRIS)
federa 1
2-A
National Response Center
Regional Response Centers
District Offices:
1st Coast Guard District
ISO Causeway Street
Boston, MA 021U
Duty Officer: 617/223-6650
2nd Coast Guard District
Federal Building
1520 Market Street
St. Louis, MO 63101
Duty Officer: 31*i/622-
-------
TABLE 6. (continued)
Information source
Interagency Reg to log-
ical Assistance Plan
(IRAP)
Organization
Federal
Type of
Information
Ass i stance
1,2
Access
1 . CHEMTREC 800/424-8300
(202/483-7616 In Washington, D.C.)
2. Regional Offices:
1.
2.
3.
k.
5.
6.
Office
Brookhaven
Area Office
Oak Ridge Oper.
Office
Savannah River
Ooeratlons
Office
Albuquerque
Operations
Office
Chicago
Operations
Office
Idaho
Operations
Office
P.O. Address
Upton L.I .
New York 11973
P.O. Box E
Oak Ridge, TN
37830
P.O. Box A
Alken, S.C.
29801
P.O. Box 5«tOO
Albuquerque
New Mexico 87115
9300 S. Cass Ave.
Argonne
Illinois 60439
P.O. Box 2108
Idaho Falls
Idaho BS'tOl
Telephone
3»i5-2200
«i80-86l7
Ext. *i510
n. August, SC
82lt-6331
Ext. 3333
26k-^667
526-0111
Ext. 1515
ODD
Area
Code
516
615
803
505
312
208
7. San Francisco
Operations
Office
8. Rlchland
Operations
Office
2111 Bancroft Way
Berkeley
California 9'»70'i
P.O. Box 550
Highland
Washington 99352
8M-5121 MS
Ext. 66k duty hrs
841-92't'i off hrs
942-73SI
509
-------
TABLE 6. (continued)
ro
Information source
Coast Guard National
Strike Force
U.S. Army Technical
Escort Center,
Chemical Emergency
Response Team
Chemical Transportation
Emergency Center
(CHEMTREC)
Pesticides Safety
Team Network
Transportation Emer-
gency Assistance Plan
(TEAP)
Type of
Organization
Federal
Federal
Privately
sponsored
Privately
sponsored
CanadIan,
privately
sponsored
Type of
Information
Assistance3
2,3
,2,3
,2,3
Access
National Response Center
(800/424-8802)
Dept. of Army Operation Center
703/521-2185
Through CHEMTREC 800/424-9300
(in Washington, D.C. 202/483~76l6)
Through CHEMTREC 800/424-9300
(in Washington, D.C. 202/483-7616)
Each regional Control Center has
2k hour number:
I. Hooker Chemicals Division
Vancouver, British Columbia
604/929-3441; geographic location;
British Columbia
2. Celanese Canada Ltd., Edmonton,
Alberta 403/477-8339; geographic
location: Prairie Provinces
3. Canadian Industries Ltd., Copper
Cliff, Ontario 705/682-2881
geographic location: Northern
Ontario
-------
TABLE 6. (continued)
Information source
Organization
Type of
Information
Assistance3
f-o
cc
Access
A. Dow Chemical of Canada, Ltd.,
Sarnia, Ontario 519/339-37U
geographic location: Central Ontario
5- Cyanamid of Canada, Ltd., Niagara
Falls, Ontario; 416/356-3310
geographical location: Eastern
Ontario
6. DuPont of
Ontar io;
locat ion:
Canada, Ltd., Maitland,
613-3^8-3616; geographical
Western Ontario
Chlorine Emergency
Plan (CHLOREP)
Privately
sponsored
1,2,3
7. Allied Chemical Canada Ltd.,
Valleyfield, Quebec, 5H-373-8330
geographical location: Quebec -
south of St. Lawrence
8. Gulf Oil Canada Ltd., Shawinigan,
Quebec, 819-537-1123; geographical
location: Quebec, north of St.
Lawrence
Through CHEMTREC - 800/*»2^-9300
(in Washington, D.C. 202/^83-7616
'1. Respond to scene with trained personnel if required.
2. Provide information on identity, hazards, or what to
3. Refer to knowledgeable contact
do.
A. On-line computer available.
-------
TABLE 7. INFORMATION RETRIEVAL SYSTEMS
Information source
On-1Ine
computer
system Contact
M
Lockheed Information yes
Systems
Edltec Inc. yes
Illinois Institute for Environ-
mental Quality Library yes
Institute for Scientific
Information yes
NIOSH Technical Information
Center yes
National Technical Infor-
mation Service yes
National Emergency Equipment
Locator System (NEELS-Canadlan) yes
National Analysis of Trends in
Emergencies System (NATES-
Canadtan) yes
NASA - Scientific £ Technical
Information Office yes
NASA - Indus. Applications Cntrs:
Univ of Conn,, Storrs, Ct. yes
Research Triangle Park, NC yes
Univ of Pittsburg, PA yes
Indiana Univ, Bloomington, IN yes
Univ of N. Mexico, Albuquerque yes
Univ. of S. Cal, Los Angeles, CA yes
415/493-441!
Ext. 45635
312/427-6760
312/793-3870
215/923-3300
301/443-3063
202-967-4349
819-997-3742
819/997-3742
202-755-3548
203/486-4533
919/549-8291
412/624-5211
312-337-8884
505/277-3622
213/746-6132
Information Source
Global Engineering
Documentation Services
U.S. Dept. of Commerce
Maritime Administrator
National Bureau of Standards
Fire Technology Library
NASA/Aerospace Safety
Research 6 Date Institute
Chemical Abstract Service
Ohio State University
Computer Search Center
Illinois Institute of Tech.
Research Institute
Fire Research Section
Southwest Research Institute
Environmental Engineering
Dlv., Texas A&M University
Toxicology Data Bank, Nat!
Library of Medicine
On-1Ine
computer
system Contact
no
714/540-9870
213/624-1216
no 212/967-5136
no 301/921-3246
no 216/443-4000
Ext. 285
no 614/421-6940
no 312/225-9630
no 512/684-5111
Fxt. 2415
no 713-845-3011
no 301-496-1131
-------
*1. TADS Accession No.
2. Material Name
3. Synonyms
k. Trade Names
5. Chemical Formula
•••6. Species in Mixture
7. SIC Code
8. Common Uses
*9. Rail (I)
*10. Barge (%)
*11. Truck (%)
*12. Pipeline (*)
13. Containers
14. Shipment Size
15. General Storage Procedures
'•16. General Handling Procedures
*17« Personal Safety Precautions
18. Production Sites
-'-19- Use Areas
20. Hydrolysis Product Of
»21. % Additive
22. Flammability
23. Explosiveness
2k. Ai r Pollution
*25. Action Levels
•C26. Field Detection, Limit (ppm) Techniques
*27- Laboratory Detection Limit (ppm), Techniques
28. Major Hazards
29. Standard Codes
30. Melting Point (°C)
31. Melting Characteristics
32. Boi1 ing Point (°C)
33- Boiling Characteristics
3A. Solubility (ppm 25°C)
35. Solubility Characteristics
36. Specific Gravity
37. Probable location and state of material
38. Binary Reactants
39- Lower Flammability Limit U)
40. Upper Flammability Limit (%)
(continued)
(Asterisk indicates non-searchable components, for display only)
Figure I. Information segment headers In OHM-TADS.
30
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k\. Toxic Combustion Products
k2. Extinguishing Methods
43. Lower Explosive Limit (%}
kk. Upper Explosive Limit (%)
k5. Flash Point (°C)
46. Auto Ignition Point (°C)
k~J. Inhalation Limit (Value)
k&. Inhalation Limit (Text)
**9. Irritation Levels (Value)
50. Irritation Levels (Text)
51. Di rect Contact
52. General Sensation
53^ Lower Odor Threshold (ppm)
5k. Lower Odor Threshold (Text)
55. Medium Odor Threshold (ppm)
56. Medium Odor Threshold (Text)
57- Upper Odor Threshold (ppm)
58. Upper Odor Threshold (Text)
59. Lower Taste Threshold (ppm)
60. Lower Taste Threshold (Text)
61. Medium Taste Threshold (ppm)
62. Medium Taste Threshold (Text)
63- Upper Taste Threshold (ppm)
6k. Upper Taste Threshold (Text)
65. Corrosiveness
66. Synergistic Materials
67. Antagonistic Materials
68. Degree of Hazard to Public Health
69. Exchange Capacity with Natural Soils
70. Industrial Fouling Potential
71. Effect on Water Treatment Process
72. Direct Human Ingestion (mg/kg wt)
••'73. Reference for Direct Human Ingestion
74. Recommended Drinking Water Limits (ppm)
"75. Reference for Recommended Drinking Water Limits
76. Body Contact Exposure (ppm)
•;77. Reference for Body Contact Exposure
78. Fresh Water Toxicity
79- Limiting Water Quality
80. Salt Water Toxicity
81. Animal Toxicity
82. Livestock Toxicity (ppm)
"83. Reference for Livestock
Qk. Waterfowl (ppm)
(continued)
Figure I (continued).
31
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*85. Reference for Waterfowl
86. Aquatic Plants (ppm)
*87. Reference for Aquatic Plants
88. Irrigable Plants (ppm)
*89. Reference for Irrigable Plants
90. Major Species Threatened
91. Acute Hazard Level
92. Etiological Potential
93. Emergency Water Quality Std (ppm)
94. Prolonged Human Contact (ppm)
*95. Reference for Prolonged Human Contact
96. Potential for Accumulation
97. Chronic Aquatic Toxicity Limits (ppm)
*98. Reference for Chronic Aquatic Toxic Limit
99. Taste Imparting Characteristics (ppm)
*100. Reference for Taste Imparting Characteristics
101. Chronic Animal Toxicity Limits (ppm)
*102. Reference for Chronic Animal Toxicity Limits
103. Chronic Waterfowl Toxicity Limits (ppm)
*10^. Ref. for Chronic Waterfowl Toxicity Limits
105. Chronic Plant Toxicity Limits (ppm)
*106. Ref. for Chronic Plant Toxicity Limits
107. Soil Transformation Properties
108. BOD (Ib/lb)
109. In Situ Amelioration
110. Beach and Shore Restoration
"111. Availability of Countermeasure Material
112. Disposal Methods
*113. Disposal Notification
11^. Chronic Hazard Level
115. Food Chain Concentration Potential
116. Persistency
117- Major Water Uses Threatened
118. Adequacy of Data
119- Carcinogen!city
120. Mutagenicity
121. Teratogentcity
122. Color in Water
123. Fields Containing Data
Figure I (continued)
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2.2.3 Access
Access to OHM-TADS is through the oil and hazardous material spill coordina-
tor at the EPA Regional office (Regional Response Center).
2.3 U.S. COAST GUARD CHRIS
2.3.1 Description
This system consists of four manuals, a regional contingency plan, a hazard-
assessment computer system (HACS) , and an organizational entity at the Coast
Guard Station. The four manuals are as follows:
Vol. l-CG-446-1 - Condensed Guide to Chemical Hazards - contains
essential information on those hazardous chemicals that are shipped in
large volumes by marine transportation.
Vol. 2-CG-M6-2 - Hazardous Chemical Data Manual - contains detailed
i-nformation on the chemical, physical, and toxicolog ical properties of
hazardous chemicals, in addition to all the information in Vol. I.
Vol. S'CG-MS-S - Hazard Assessment Handbook - contains methods of
estimating the rate and quantity of hazardous chemicals that may be
released and methods for predicting the potential toxic, fire, and
explosive hazards.
Vol. 4-CG-446-4 - Response Methods Handbook-contains information on
existing methodology for handling spills; the Appendix to this volume
contains a list of manufacturers of equipment which may be useful in
a spill si tuat ion.
The contingency plan is part of the National Contingency Plan as mentioned
in Chapter 1. The Hazard - Assessment Computer System is the computerized
counterpart of Volume 3 and makes it possible to obtain detailed hazard
evaluations. Although calculations can be performed by hand using Vol. 3,
the HACS permits one to make a more complex and usually more accurate assess-
ment of the spill situation.
2.3.2 Mode of Operation
Volume 1, Condensed Guide to Chemical Hazards, is intended for use by
port security personnel and others who may be first to arrive at the
scene of the accident. It contains easily understood Information about
the hazardous nature of the chemical, assuming the chemical is Identified.
It is intended to assist those present In quickly determining the actions
that must be taken immediately to safeguard life, property and the
environment. Volume 1 contains a list of the information needed to assess
potential hazardous effects through the use of Volume 3-
Volumes 2, 3, and 4 are Intended for use by the On-Scene Coordinator's
(OSC) office and the Regional and National Response Centers. Coast
33
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Guard stations, especially those in major ports, will usually also have
these manuals. The computer system (HACS) is also designed for use by OSC
personnel.
Volumes 2 and 3 are designed to be used together. For example, Vol. 2
The Hazardous Chemical Data Manual contains a hazard-assessment code for
each chemical. This code is used in Vol. 3 The Hazard-Assessment Handbook
to select the appropriate calculation procedures for the hazard assessment,
enabling the user to estimate the rate and quantity of hazardous chemicals
that may be released under different situations. For example, procedures
are provided for estimating the concentration of hazardous chemicals (both
in water and in air) as a function of time and distance from the spill.
The Hazard-Assessment Computer System (HACS) is the computerized counter-
part of Vol. 3 and makes it possible to obtain detailed hazard evaluations
quickly. The HACS system is intended primarily for use by OSC personnel
through Coast Guard headquarters. While the input needed for evaluation
will depend on the specific accident situation and that part of the system
which is to be used, the following information should be supplied to Coast
Guard headquarters as applicable.
Material discharged
Quantity spilled
Quantity originally in tank
Location of spil1
Time of occurrence
Tank dimensions
Other cargos or nearby chemicals
Hole diameter
River depth
River width
Stream velocity
Temperature (air)
Temperature (water)
Cloud cover (percent)
Depending on which model it is decided to use, other information may be
needed by Coast Guard headquarters. In this case a call back number should
be given so that headquarters personnel can request additional information
if necessary. More information on the use of Vol. 3 is given in Chapter 3
of this report.
Volume **, The Response Methods Handbook, contains descriptive and technical
information on methods of spill (primarily oil) containment. This manual is
intended for use by Coast Guard OSC personnel who have had some training or
experience in hazard response.
2.3.3 Access
Access to the CHRIS manuals can be obtained through the Coast Guard District
office (see Table 6). The HACS can be assessed on an emergency basis
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through the Regional Response Center, the Coast Guard District office, or
directly through the Department of Transportation National Response Center
at Coast Guard headquarters.
2.4 INTERAGENCY RADIOLOGICAL ASSISTANCE PLANT (IRAP)
2.4.1 Description
The Interagency Radiological Assistance Plan (IRAP) is designed to assist any
person in obtaining technical guidance In coping with radiation emergencies.
It operates through the U.S. Energy Research and Development Administration
but works closely with other Federal, state, military, and regional groups.
In the IRAP the U.S. is divided into eight geographical areas of responsi-
bility each with a regional coordinating office. These areas and the offices
with telephone numbers are given in Table 6.
2.4.2 Mode of Operation
Upon receiving an emergency call, the regional coordinator investigates the
situation to assess the potential radioactive hazard. He tries to get as
much information over the phone on the specifics of the situation and the
type of material (e.g. from the shipping papers). Advice will be given over
the phone if the potential hazard appears minimal. If the spill or leak
appears serious, a technical response team will be dispatched. This team
will work jointly with state personnel (civil defense, public health) when-
ever possible. In any case the coordinating office will notify the appro-
priate state office of the radioactive spill. When the response team is
dispatched, the Nuclear Regulatory Commission is notified especially if the
spilled material is licensed. The main functions of the response team are to
assess the hazard, to inform people of the hazard, and to recommend emergency
actions to minimize the hazard. The responsibility for clean-up rests with
the shipper or carrier (the party who has possession of the material at the
time of the spil1).
2.4.3 Access
Access to the IRAP is through the regional coordinating offices given in
Table 6. Each office has a 24-hour emergency telephone number. When
reporting an incident, the following information should be given:
1. Name and title of caller
2. Cal1 back number
3. Location and magnitude of problem
4. Information of shipping papers
type of material
manufacture or shipper
carrier
IRAP can also be accessed through CHEMTREC.
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2.5 U.S. COAST GUARD NATIONAL STRIKE FORCE
2.5.1 Description
The Coast Guard's National Strike Force (NSF) is part of the National
Contingency Plan established under authority of the Federal Water Pollution
Control Act Amendments of 1972, Section 311 (1). It consists of high-seas
equipment and trained personnel available to assist the On-Scene Coordinator
upon request during Phase 111 (Containment and Countermeasures), Phase IV
(Cleanup, Mitigation and Disposal), and Phase V (Documentation and Cost
Recovery), as defined in the National Contingency Plan. There are three
Coast Guard Strike Teams located on the East, West, and Gulf coasts. Each
strike team consists of 18 or 19 men, including 3 or ^ officers. Each
strike team is capable of responding to a pollution incident in its area
with four or more men within 2 hours and at full strength in 12 hours. The
Str.ike Team can provide communications support and assistance and advice on
ship salvage, diving and removal techniques. Available equipment primarily
designed for air transport, consists of the following:
1. Air Deliverable Antipollution Transfer System (ADAPTS),
consists of a pumping system to off-load stricken cargo
vessels.
2. Yokohama fenders, used for side protection during vessel-
to-vessel cargo transfer.
3. High-seas containment barrier.
k. High-seas skimmer,
2.5.2 Access
The services of the National Strike Force are available to any On-Scene
Coordinator anywhere in the country. Requests for assistance can be made
through the National Response Center through its 2^-hour emergency tele-
phone number (see Table 6). The specific details of the emergency situa-
tion should be given.
2.6 U.S. ARMY TECHNICAL ESCORT CENTER CHEMICAL EMERGENCY RESPONSE TEAM
2.6.1 Descri pt ion
The U.S. Army Technical Escort Center maintains, on standby, a 14-man alert
team at Aberdeen Proving Ground, Maryland, ready to respond to chemical
emergencies within 2 hours. If necessary, additional personnel are available
for mobilization. The team is trained and experienced in handling chemical
emergencies and has available to it special equipment such as decontamination
trucks, detection devices, and protective clothing.
36
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2.6.2 Mode of Operation
The U.S. Army Technical Escort Center's team responds to a chemical emergency
when directed by the higher command. While the team was formed mainly to
respond to emergencies involving Department of the Army chemicals, it has
assisted other agencies such as the U.S. Coast Guard.
2.6.3 Access
To obtain the assistance of the escort team, initial contact should be made
with the regional EPA office. EPA personnel will then contact the Dept. of
the Army Operations Center at the commercial number listed in Table 6. Upon
receipt of each request, the Army Operations Center determines if the
specific services of the Technial Escort Center are needed. If the determi-
nation is made for the emergency team to respond, intermediate commands are
notified and the team dispatched. The Commander of the Technical Escort
Center should be contacted.
2.7 CHEMICAL TRANSPORTATION EMERGENCY CENTER (CHEMTREC)
2.7.1 Description
CHEMTREC serves a clearinghouse function by providing a single emergency
24-hour telephone number for chemical transportation emergencies. Upon
receiving notification of a spill, CHEMTREC immediately contacts the shipper
of the chemicals involved for assistance and follow-up. CHEMTREC also pro-
vides warning and limited guidance to those at the scene of the emergency
if the product can be identified either by the chemical or trade name. The
CHEMTREC system covers over 3,600 items which have been submitted by manu-
facturers as their primary items of shipment. CHEMTREC is sponsored by the
Manufacturing Chemists Association although non-members are also served.
The system is not computerized.
2.7.2 Mode of Operajjon_
The CHEMTREC emergency telephone number is widely distributed to emergency
service personnel, carriers, and throughout the chemical industry. The
number is usually given on the bill of lading. When an emergency call is
received by CHEMTREC, the person on duty records the essential information in
writing. He tries to obtain as much information as possible from the caller.
The person on duty will give out information as furnished by the chemical
producers on the chemical(s) reported to be Involved. This would include
information on hazards of spills, fire, or exposure. After advising the
caller, the person on-duty immediately notifies the shipper of the chemical
by phone, giving him the details of the situation. At this point, respon-
sibility for further guidance passes to the shipper.
37
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CHEMTREC'S function is basically to serve as the liaison between the person
w ththe problem and the chemical shipper and/or manufacturer the theory
being tha? the manufacturer of the chemical or material will know the most
about his product and its properties. CHEMTREC also serves as a contact
potnt for the Chlorine Institute, the National Agncultura Chemicals
Association (pesticides), and the Energy Research and Development Admin is-
tration (radioactive materials).
2.7.3 Access
CHEMTREC can be accessed through its emergency telephone number listed in
Table 6. As much of the following information should be provided by the
caller as possible:
1. Name of caller and call back number.
2. Location of problem.
3. Shipper or manufacturer
k. Container type
5. Rail car or truck number
6. Carrier name
7. Consignee
8. Local conditions
2.8 NACA PESTICIDES SAFETY TEAM NETWORK
2.8.1 Description
The National Agricultural Chemicals Association through its members
operates a national pesticide information and response network. Its
function is to provide advice and on-site assistance when the spill
situation warrants it.
2.8.2 Mode of Operation
The network operates through the CHEMTREC office. Upon receiving
notification of an emergency involving a pesticide, the manufacturer is
contacted by CHEMTREC. The manufacturer will provide specific advice
regarding the handling of the spill. If necessary, spill response teams
are available on a geographical basis to assist at the emergency scene.
2.8.3 Access
Access to the network is through CHEMTREC (see Table 6 for telephone no.)
38
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2.9 TRANSPORTATION EMERGENCY ASSISTANCE PLAN (TEAP), Canadian Chemical
Producers' Association (CCPA)
2.9.1 Description
TEAP serves a function in Canada similar to that of CHEMTREC In the U.S.
Canada Is divided into eight geographic areas, each served by a regional
control center. Depending on the location of the spill, one of these
control centers is called and notified of the emergency. The functions
of TEAP are to provide emergency advice, to get knowledgeable personnel
(usually the manufacturer) in touch with responsible people at the
emergency scene, and to see that on-the-scene assistance is provided
i f needed.
2.9.2 Mode of Operation
When a call is received at a regional control center, the attendant
records basic information on a record sheet and obtains a call-back
number. He may also give preliminary Information from standard
references if the name of the product Is known. The attendant will then
call one of the center's technical advisers with the preliminary
information. The technical adviser will then call the accident scene
to determine as much detail as possible. At this time he may also be
able to provide additional advice on coping with the emergency. The
adviser will then try to contact the producer from the listed
references. If the producer can be contacted, the adviser will turn
the problem over to them as the most knowledgeable contact. If the
producer cannot be reached, or if distances are great, the regional
control centers will contact a company familiar with the product. The
center is also prepared to send men and equipment to the scene if
necessary. Once contact has been established between the producer and
the local authorities on the scene, the technical adviser assumes a
follow-up role and notifies the CCPA of the incident.
2.9.3 Access
Access to TEAP is through the regional control centers given in Table 6.
Essential information that should be provided Includes:
1. Exact name of the product spilled
2. Name of the producer
3. Name of the carrier
2.10 CHLORINE EMERGENCY PLAN (CHLOREP)
2.10.1 Description
Chlorine manufacturers in the U.S. and Canada through the Chlorine
Institute have established the Chlorine Emergency Plan to handle
chlorine emergencies. This is essentially a mutual aid program whereby
the manufacturer closest to the emergency will provide technical
assistance even if it involves another manufacturer's product.
39
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2.10.2 Mode of Operation
The CHLOREP system operates through CHEMTREC. Upon receiving an emergency
call, CHEMTREC notifies the appropriate party in accord with the mutual
aid plan. This party then contacts the emergency scene to determine if
it is necessary to send a technical team to provide assistance. Each
participating manufacturer has trained personnel and equipment available
for emergencies.
2.10.3 Access
Access to CHLOREP on a 2^-hour basis is through CHEMTREC (telephone
number i n Table 6).
2.11 INFORMATION RETRIEVAL SYSTEMS
Organizations providing information retrieval should be considered as
secondary sources of information because information is from the published
literature or past events, and because interaction is limited since the
contact usually has no special expertise in spills technology or hazardous
chemicals. A list of information retrieval sources was given in Table 7.
Because of the emergency nature of most spills, a short response time
is important. In this regard an on-line computerized system is desirable,
although a manual search could also have a short turnaround time. Data
bases range from spill specific to general scientific. Examples of
specific bases are the Canadian NEELS data base which covers the location
of publicly and privately owned cleanup equipment and the NATES data
base which covers the history of past spills and their cleanup. These
two systems are discussed below.
The mode of operation for the computerized systems involves inputting
applicable key words as search components. These might include the name
of the chemical and words such as "pollution", "water", "removal",
"toxicity", "reactivity", and "hazards".
2.12 NATIONAL EMERGENCY EQUIPMENT LOCATOR SYSTEM (NEELS)
2.12.1 Description
NEELS is an on-line computer system designed and operated by the
Environmental Protection Service (EPS), Environment Canada. Its function
is to provide information on equipment available near the spill scene
which may be useful. This includes containment and treatment equipment
held both publicly and privately.
2.12.2 Mode of Operation
Connection can be made with the NEELS computer system through any EPS
regional office. The longitude and latitude of the spill must be entered
-------
as input and the desired output must be selected from the following
choices:
1. All equipment at the nearest location.
2. Nearest specific type of equipment.
3. Nearest particular piece of equipment.
Depending on the selection, the computer prints out the location of the
equipment and the name of the person and telephone number to call.
2.12.3 Access
Information on gaining access to NEELS can be obtained from the National
Environmental Emergency Center by calling the 24-hour emergency number
1 is ted in Table 6.
2.13 NATIONAL ANALYSIS OF TRENDS IN EMERGENCIES SYSTEM (NATES)
2.13.1 Description
NATES is an on-line computer system designed and operated by the
Environmental Protection Service (EPS), Environment Canada. Its function
Is to provide information on how a similar spill was handled.
2.13.2 Mode of Operation
Connection can be made with the NATES computer system through any EPS
regional office. Main input to the system is the type of material
spilled. Output includes data on location, date, material spilled, cause,
environment including site conditions and contingency plans, cleanup
including method used, weather, agencies involved, legal actions, and
cost.
2.13.3 Access
Information on gaining access to NATES can be obtained from the National
Environmental Emergency Center by calling the 24-hour emergency number,
1isted in Table 6.
2.14 USEFUL GUIDES AND REFERENCE HANDBOOKS
There are many handbooks and reference texts which may prove helpful in the
event of a hazardous material spill. Any person who may be confronted with a
spill emergency should have access to one or more of the commonly used
references. In addition, the Regional Response Center maintains a hazardous
materials reference library. In particular, the references listed in Table 8
should be available.
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TABLE 8. REFERENCES TO USE IN CONJUNCTION WITH THIS MANUAL
Critical References
OHM-TADS Data Sheets
CHRIS Manuals \-k (CG-M6-I-4)
Regional Contingency Plan
Regulation for Shipping Hazardous Materials
^3 CFR-Code of Federal Regulations,
Transportation Vol. k^ Pts. 170-182
FAR 103-Federal Aviation Regulations Vol.
VI Pt. 103
CAB o2-0fficial Air Transport Restricted
Articles Tariff No. b-D
I ATA-Internalional Air Transport Association
Restricted Articles Regulations
tPA Field Detection and Danger Assessment
Manual for Oil and Hazardous Material Spills
Official Motor Freight Directory
Official Railway Guide
Dangerous Properties of Industrial Materials, by
N. Irving Sax
Critical Reference Source
US EPA Office of Hazardous Materials, Wash. DC
20*»GO.
US Gov't Printing Office, Wash. DC 20^02.
US EPA-Regional Environmental Emergency Section.
US Dept. "of Transportation Office of Hazardous
Materials.
US Dept. Federal Aviation
US EPA Office of Water anJ Hazardous Materials
Wash., DC 20400.
Van Nostrand Reinhold Co., 450 W. 33rd Street,
New York, NY 10001
Chemical Transportation and Handling Guide
RSMA, 181 E. Lake Shore Drive, Chicago, IL 60611
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TABLE 8. (continued)
Critical References
Laboratory Waste Disposal Manual
Recommended Methods of Reduction, Neutralization,
Recovery or Disposal of Hazardous Waste (Vol. 1-16)
by TRW Systems Group
Hazardous Chemicals Data
Critical Reference Source
Manufacturing Chemists Association, 1825
Connecticut Ave. N.W., Wash., DC 20009.
NTIS
US Dept. of Commerce
Springfield, VA 22151.
National Fire Protection Association
470 Atlanta Ave.
Boston, MA 02110
Desirable References
10
Merck Index
Chemical Rubber Corporation, Handbook of Chemistry
and Physics, CRC Press
Handbook of Chemistry - Handbook Publishers Inc.
by NA Lange
Behavior of Organic Chemicals in the Aquatic
Environment - Part I - A Literature Critique,
Manufacturing Chemists' Association
Behavior of Organic Chemicals in the Aquatic
Environment - Part II - Behavior in Dilute Solu-
tions, Manufacturing Chemists' Association,
April 1968
1963 Census of Manufacturers - Location of Manu-
facturing Plants by Industry, County, and Employ-
ment Size
Chemical Data Guide for Bulk Shipment by Water,
US Coast Guard, 1966
Chemical Engineers' Handbook, Perry, John H.,
et al., eds., £ 5th ed., 1973
Chemical Safety Data Sheets (SD-1 - SD-96),
Manufacturing Chemists' Association
Handbook of Analytical Toxicology, Sunshine,
I., ed., Chemical Rubber Co., 1969
MCA Chem-Card Manual
Mineral Facts and Problems, US Bureau of Mines
Bull. 630, 1965
Organic Chemistry, Morrison, R.T., and R.N. Boyd,
2nd ed., 1966
Orsanco Quality Monitor, July 1970
Orsanco Quality Monitor, July 1970
The Pesticide Review, US Dept. of Agriculture,
1970
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TABLE 8. (continued)
Desirable References
Hygienic Guide Series, American Industrial
Hygiene Association
Pesticide Poisoning Of Pond Lake, Ohio, Investi-
gation and Resolution (for the EPA, Ryckman,
Edgerly, Tomlinson and Associates, Inc.
Proceedings of Conference On Hazardous Cargos,
(US Coast Guard) July, 1970, New London, CT
Proceedings Of the 1972 National Conference On
Control of Hazardous Material Spills (For the
EPA) University of Houston, Houston, TX
Spill Prevention Techniques For Hazardous Pollut-
ing Substances, (For the EPA), Arthur D. Little Co.
Standard Methods For the Examination of Water
and Wastewater, American Public Health Association,
American Public Water Works, and Water Pollution
Control Federation
Water Quality Criteria, McKee, J.E. and H. W.
Wolf, The Resources Agency of California, State
Water Quality Control Board
Water Quality Criteria - Report Of the National
Technical Advisory Committee To the Secretary Of
The Interior, April 1, 1963, F.W.P.C.A., Wash.
Pollution and Marine Ecology, Olson, T.A., and
R.J. Burgess, 1967
Railroad Accident' Report - Southern Railway Com-
pany Tranin 154 Derailment with Fire 6 Explosion,
Laurel, MS., Jan. 25, 1969
Safety Guides (SG-1 - SG-19) Manufacturing
Chemists' Association
Spillages of Hazardous Chemicals (Chart)
Water Pollution Abatement Manual, Manuals Sheets
W-l, W-2, W-3, W-4 & W-6, Manufacturing Chemists'
Association
Waterborne Commerce of the United States, US
Corps of Engineers, Parts 1-5, 1968
Control of Spillage of Hazardous Polluting Sub-
stances, 15090 FOZ (for the EPA), Battelle
Memorial Institute
Dangerous Articles Emergency Guide, Bureau of
Explosives, Association of American Railroads
Explosives and Other Dangerous Articles, Bureau
of Explosives, Association of American Railraods
Fire Protection For Chemicals, Bahme, C.W.,
National Fire Protection Association
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3-0 - CHAPTER 3 - IDENTIFICATION AND ASSESSMENT
3.1 GENERAL
The information in this chapter deals with stepwise identification and
assessment of the danger potential in a spill situation. The material pre-
sented has been divided into two parts which are directed at two people
associated with the spill control effort. One person is called the flan
on the Scene (MOS) who is the on-scene coordinator for the region or his
designated representative at the spill site. The MOS is to provide infor-
mation to a remote On-$cene Coordinator who has available to him the
additional information critical to accurate spill identification and
assessment. This Manual provides the remote OSC with directions for using
information provided by the MOS and directing his further activity.
3.2 DIRECTIONS FOR THE MAM ON THE SCENE
3.2. I Assun£.t JL°n_s_
There are various assumptions inherent in this presentation of the duties
of the ilOS. These assumptions include:
I. The Man on the Scene (MOS) is the on-scene coordinator or his designa-
ted representative at the site of a spill situation. The MOS is
aware of the risks involved in spill control.
2. The responsibility of the MOS is to provide information to a remote
OSC which will aid in spill identification and assessment of the
human danger potential.
3- The responsibility for evacuation, fire fighting, or crowd control is
not the duty of the appointed MOS but is assigned to other agencies,
divisions, or personnel.
4. More than one person is available to perform the functions of the
MOS, if necessary. Therefore, notification can be done concurrently
with information gathering for identification.
3.2.2 Safety
The safety of the people who arrive on the scene of a hazardous spill is
critical to consider'before any action is taken. All spills are con-
sidered extremely hazardous. If the identity of the spill is not known,
then the MOS should not approach the spill and should await the arrival
of more highly trained, experienced personnel or a volunteer who is more
aware of the risks involved with hazardous materials. In /ill cases, fully
protective clothing should be worn by personnel at the spill site. In
addition, the following general safety precautions should be followed:
I. Always approach a spill from upwind.
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2. Don't touch the material and avoid any indirect or direct contact
with it.
3. Remove all possible ignition sources. Do not smoke.
4. Restrict access to the area.
5. Do not touch any container unless full knowledge of the hazards
involved is available.
6. If unidentified fuming liquids or gases are present, do not approach.
3.2.3 Identification Procedures - MOS
3.2.3.1 General - The MOS is the eyes and ears of a remote OSC. There are a
series of steps to follow which will allow the MOS to specifically gather
sufficient information for transfer to the OSC so an identification can be
made.
3.2.3.2 Establish the type of soil - The first step is to
determine what type of spill is involved by identifying the source of the
spill. The following types of spills are possible:
a. Trains e. Ship f. Barge
1. Tank car 1. Dry Cargo
2. Box car 2. Tank Ship 9< -
b TrUrl« 3. Com. Pass. Vessel
Vessel
2* Trailer 5' CG Vessel h- Storage Tank
6. Pleasure Craft 1 . Offshore
c- Bus 7. Tugboat 2. On Shore
d. Aircraft 8> Unidentif'ed 3. Other
1 . Cargo
2. Passenger
Once the location and source of spill has been specified, the MOS should
refer to the specific Figure (no. 2-12) which allows him to answer pertinent
questions that lead to identification.
3.2.3.3 Notation of visible_Jab_ej_ - There are two types of package labels. (2)
The MOS should answer the following questions if the packages can be safely
investigated:
1. Are any warning labels visible?
-------
1. Are any of the following hazardous placards or labels visible on the
train car: (2)
KEEP
,' LIGHTS
HANDLE CAREFULLY
EXPLOSIVES
HANDLE CAREFULLY
KEEP FIRE AWAY
DO NOT REMAIN ON OR NEAR
THIS CAR UNNECESSARILY
POISON GAS
(FOR TANK CARS I
DO NOT REMAIN ON OH NEAR
THIS CAR UNNECESSARILY
POISON GAS
I FOR TANK CARS I
CAUTION
This Car Contains
POISON GAS
Beware of Fumes from Leaking
Packages.
(FOR OTHER THAN TANK CARS)
DANGEROUS
EMPTY
DANGEROUS
EMPTY
DANGER
FUMIGATED or
TREATED
2. If so, what is the contents identification on the placard?
3.
k.
5.
6.
What is the identification, number and type of the car?
ID No.
Other
TYPE: Tank
Boxcar
Can the waybill (freight bill) be obtained from the conductor, in the
engine or in the caboose? (3) (Typical waybill in Figure 3)
Yes No
If yes, what is the office of the dispatcher? (Get information from
train conductor if possible.)
What is the train's location?
a. Railroad track owner
(name on engine or caboose)
b. Nearest town and distance
c. Nearest railroad milepost
d. Distance from nearest:
Highway, and
Highway number
Figure 2. Identification questions for train spills.
-------
,' H . 5 f-' L M ._ i.' - N D U M
CARRIER _______ _ _r_.f-_:
At MILWAUKEE. WIS.
_____ 19
-. ____ -- <•'--*. -^-:'.-~ ."--- ------ ..... -
From REXNORD INC. CHA"tfv?s?iJ-vVEVOR
Consigned ,e U.S. STCL'L C03P
CAL ATLAS
DIVK At T!?: 'c
." L- _v far
CHUTES OR SPOUTS NOI IRON
7 ga or thicker
CHAIN AND STEEL FLIGHTS ASSEMBLED
Jt
FLIGHTS, STEEL 1 A
FLIGHTS, CONVEYOR. fffOOflEN
PLASTIC AFHCLES NOI e/1 iiiiWM
Dwtanri tasMi 1 »T F
Tbt rufttHl klDta| *t /
RAILS - BAR IRON I/S NOI
OR FORMS NOI I/S
fabricated from material
3/16" or thicker
BOLTS OR NUTS NOI
Iron or atecl
59*770#
^ /
•^
.-,0/
V
/
RECEIVED A
MITCH
C. 4 N. \
MAY :
fenttS Uailo
StiiDoers li
i- .«,,„ - „ „ .... -,
recourse on the con«,gnor me COIBUJIOF
iriili sign me lollcwmg itaiemenT
REXNORD INC
PREPAID
Received $
^'J^1 *9en'
Cnargvt
advanced X
• II me ahipmani mcnres between two
porli by • carrier by water Ifie law
r«flulr«s mat the Bril ol Lading shall male
NOTE - Wtora me rale a OecwrKJoni on
v#lue ihrpperl are raqurred lo stale
ip*crtic«tty «i wrNing me agreed or de-
Clirefl vatua Of ttw properry
TrM>«r**dordacUr«d oalue of (TM prop-
erty la hM*br aawclflcaKy >ut«d bf KM
•hlppor to be no4 eicMdtnJB.
rMILWAUKfX
:LL BELT
^TRANSP
** /
J21975^^
nn 7 nf 1 (rat ri™0fc*r/*f
« Bill of LJTJJBC '
3tf raif CoiHrt
. . E-F-MVARaAGEMT
CAPY
L7 WT 55500!
52* o" GQN ORDERED
6* GON FURNISHED
BLOCKING FREE
NON-DI KENSIONAL-LOAO
CAR INSPECTED & APPROVED FOR SHIPI-CNT
^ C4NW R.R.
*^a/3
CHAIN»COMVEVOB
OTVISXM
Per,
T.
Shipper.
Ptairt I fc
.Per_
Permanent posl-oftice address Dipper 4751 f "Vxnflatd Air*-, MILWAUKEE, WIS. 53214
"Agent
FORM HB35 C&C (4-73)
Figure 3. Typical freight bill for rail shipment.
-------
1. What Placards are visible? (2)
EXPLOSIVES A
Placard any quantity of Explosives A
or combination of A & B Explosives.
See DANGEROUS for mixed loads.
EXPLOSIVES B
Placard any quantity of Explosives B.
Use EXPLOSIVES A placard if mixed
with Explosives A materials. For other
mixed loades see DANGEROUS
Placard 1000 pounds or more gri
weight of Nonflammable Compre
Gas.
FLAMMABLE
Placard 1000 pounds or mo
of either Flammable Solids,
Flammable Liquids or
FLAMMABLE
GAS
Placard 1000 pounds or more gross
weight of Flammable Compressed Gas.
CORROSIVES
Placard 1000 pounds or moi
weight of Corrosive Liquids.
COMBUSTIBLE
Placard when packaging] exceed
110 gallon rated capacity
(No Label Specified)
CARGO FIRE-AVOID WATER
To be used only with another Placard.
Placard to be used when so stated
on shipping papers or when
appropriate (No Label Specified!
POISON
Placard any quantity of Poison
Poison Class "A" and "B".
Placard 1,000 pounds or more
gross weight of Poison Class "B"
For mixed loads see DANGEROUS
OXIDIZERS
Placard 1000 pounds or more gross
weight of Oxidizing Material.
RADIOACTIVE
Placard any quantity
of shipments bearing
radioactive yellow
III label.
No placard required for material
bearing "radioactive — white I"
or "radioactive yellow II" labels
For mixed loads, see DANGEROUS.
DANGEROUS
Use the DANGEROUS placard
for mixed loads containing more
than one kind of hazardous mate-
rial requiring placards when the
aggregate gross weight totals 1000
pounds or more.
\MHWCTIVI
III/
Double placarding should be used
when loads requiring the
DANGEROUS placard ate mixed
with any quantity of the following
placard to the DANGEROUS placar
Explosives A
Explosives B
Radioactive
(Yellow-Ill)
Poiso
(Class
"A")
Federal Highway Administration
Bureau ol Motor Carrier Safety
2. If possible, obtain bill of lading from driver (typical bill of lading
in Figure 5).
3. If not: Record trucking company on cab
Record truck !.D« number
and type
Record highway number
distance from nearest town
Record
Record
Record
Record
highway market
distance from road
time of accident
Figure k. Identification questions for truck spills.
-------
STRAIGHT BILL OF LADING—SHORT FORM—ORIGINAL—NOT NEGOTIABLE
RECEIVED, subjecl 1
CARRIER:
Shipper's No _
Cusl No
At MILWAUKEE. WIS.
From REXNORD INC.
eteby cerlllle* lhal he Is lamlllar wllh
itlH which governs the Iran
G'GOf ll IhlS 13
rlatlon ol Ihli
Consigned to_
Destination .
Route
-County -
AMT. $_
REMIT COD PROCEEDS TO:
REXNORD INC.
P.O BOX 50018
MILWAUKEE, WIS. 53201
Car/tir Initials
No.
Subiecl to Section 7 ol Conditions ol applicable bill of lading, it this sfiipmpnl
Ireight and all other lawful charges
REXNORD INC.
NOTE. Wnere Ihe r;
Dy the snipper lo be
is dependent on value shippers are required lo
ing the agreed or declared value ol the properly
II charges are to be
or stamp here, 'To
prepaid, wnle
be Prepaid."
r-
Package
DosisSS,i;rs
concrete mixer parts
CHUTES CONCRETE
DISTRIBUTING
TANKS-NOI-SU 1/3
16 ga. lo i" n/nsld
TANKS-NOI-SU ALUM.
18 ga. or thicker
HARDWARE NOI
STEEL
CHAINS. BELTING STEEL
D/l machine finished
SHAFTS 0/T CRANKSHAFTS
W/ftgs, bras, cplgs.
SHAFTS 0/T CRANKSHAFTS
w/o fittings
• WEIGHT
Sub 10 Corr
r-
Packages
Desvs,M*;fM
NOI I/S
MACHINERY PARTS RUBBER
NOI Plislic or Rubber
Alum, Brass or Bronze
GRADING OR ROAD
IMPLEMENT PARTS
SCARIFIERS & MIXERS
COMBINED, POWER
MOTORS ELEC-GEAR
MOTOR over Stt each
INCREASING OR REDUCING
MACHINES-gcir or ip.id over 5«
HEAT EXCHANGERS-
NOI-w or w/o metering
ALUMINUM CASTINGS
NOI w/o Inserts
*WEIGHT
"bT
Kind of
Packages
Special Warns
ELECTRICAL INSTRUMENTS
NOI
NOI or parts
SCALES. FACTORY OR WHSE
KO Auto or o/t Auto
COUPLERS-TRACTOR
TRAILER OR PARTS I/S
FflRftK IIVnilT*; flH »«'V
JIBS wood or nital
BOLTS-NUTS NO)
Iron or Steel
CASTINGS-ROUGH
I/S
RINGS, ROLLED STEEL
NOI
NOI I/S 16 ga. or thicker
NOI I/S structural
labr. from material
,-;," or thicker
GREASE, LUBRICATING
NOI
PAINT, LIQUID NOI
O/T (radal tubes or gliu]
*W£IGHT
Sub ro Corr
ra^^^Kir^rar'k t*.tf* CONSTRUCTION
REXNORD INC. MACHINERY DIV. Shipper
Per
Permanenl post-office address of shipper-
4751 W. Greenfield Aye.,
MILWAUKEE, WIS. 53214
Plant # per
.Agent
FORM H835 CMD (4-73)
Figure 5. Typical truck bill of lading accompanying shipment.
50
-------
1. Is a bus bill available from the driver? Yes
(typical bus bill in Figure 7)
No
2. If yes, obtain the bus bi51 from the driver.
3. If no, record:
bus company
bus vehicle number
highway number
distance from nearest town
name of nearest town
highway marker
distance from road
time of accident
Figure 6. Identification questions for bus spills.
51
-------
GREYHOUND BUS31LL C
DESTINATION STATION ST<
KANSAS CITY MISSOURI
«-
Tt
^YT'CTOR L. PHILLIPS CO.
•"jfr'BCTS DEPOT FOR PICKUP
NO. OF PIECES i ENV. 1; SACK |
I IBGG— hCTfCl OTHER:
CONTENTS
1 CTN M.P. 9#
OmENS,OKALWL,GHT,NrO»U»T,OK YH0500G
A A ~~ ^ OQR IN
=i=>'j<«= '_ I
REX^ORD INC
^"d^ GREENFIELD AVE.
ORIGIN C,TY . STATE MILWAUKEE, WISCONSIN
02858115 1
PHONE
D CHG. ACCT.
D DELIVERY
DECL.WJ.UE ACTLIJU. WT.
5 <£? S
CONSIGNEE NOTIF
MO DAY
CD
YEAR
5
TARIFF \VT.
TIME
A. M.
P. W.
ROUTING
INSERT EACH COf.
ABBREVIATION
JUNCTION PO
ON LtNF^ RFI
COMPANY
TO
1PANVS
AND
INT
OW
1
NO. DATE AMOUNT '
FORMO— 18RJ6-70) PRJNTEOINU &X ^SS.
*yL£i4"^^
NO.
"z-jTVW
^
C-APICS 5 ^// f/6*
A^.ANCCO *
PICK UP J
CHARGES
DJ:. \ CRY j
-H'AR^ES S
?K °' 5 . |/^
TOTAL * V IfT^
STATE t
TAX *
CO. D >
AMOUNT *
TOTAL TO , if
COLLECT » Cf-
&
lljll
fitu
:]|ij
IhM
I'Pi
5 !--•{
2= »1 :
DATE AMOUNT
Figure 7. Typical bus bill attached to package .
-------
1. Are the shipping papers available from the captain of the shfp?
Yes No
2. If yes, obtain papers from the captain.
3. If no,
1. What Is the ship's flag configuration?
2. Record the vessel Name
Number
National Ity
3. Location:
Name of nearest city
Distance from nearest city
Water body Involved
Distance from shore j
Figure 8. Identification questions for spills from marine vessels.
53
-------
1. What warning placards are visible?
a. Warning
b* Dangerous Cargo
c. No Visitors - indicates possible poisonous cargo
d. No Smoking
e. No Open Lights
f. Other
g. None
(These placards are generally 3 feet x 2 feet with black, letters
on a white background.)
2. Does the barge captain have the shipping papers?
Yes No
3. If yes, obtain these papers,
*». If no, record:
Barge Name
Barge Number
Name of Waterway
Distance from Shore
Name of Nearest City
Distance from Nearest City
Figure 9. Identification questions for spills from barges.
-------
1. Does the pilot have the shipping papers? (k)
Yes No
2. If yes, obtain these papers.
3. If no, record:
Ai r1ine of Plane
Number of Plane
Number of Nearest Highway
Highway Marker
Distance from Highway
Name of Nearest Town
Distance from Nearest Town
Time of Accident
Figure 10. Identification questions for spills from airplanes
1. Is a pipeline marker available?
2. If yes, record all information from marker.
3. i f no, record:
Name of Pipeline owner (if available)
Nearest Highway 'lumber
Distance from Highway
Highway Mile Marker
Nearest Town
Distance from Nearest Town
Time of SpiI 1
Figure 11. Identification questions for spills from plpleines
55
-------
1. Is an Identification plate attached to the tank?
Yes No
2. If yes, copy Information:
3. If no, record:
Address of spill by nearest streets
Time of spi11
k. Are any additional coding systems visible? For example:
If gas cylinders are involved, what is the color of the
cylinder?
And, what is the name of the distributor?
If chemicals are used, what is the color of the cap?
or printing
and what is the name of the distributor
Figure 12. Identification questions for spills from storage tanks
56
-------
2. Are any identifying labels visible?
(An example appears in Figure 13).
Crrtlflrnlc of A Hun I l*ol A mil vsN
Ca(OH), F.W. 74.09
Chloride (CD
Iron (F«)
Sulfolf (SO.)
Olhcr Hcovy MeluU (at Pb)
Ammonium Hydroxide ppf.
Mognciium and .". Vcili Sullr
Intolublo in HCI
0.00 \1.
0.0 17..
0.1 Or.
(1.00 I".
O..IUT',
1.0".'.
0.0 IV,
CAUTION!
Homiful dutt.
Avoid contact with tkin, or Py«».
Do not breathe dost.
In cai^ of contact, immediately fluih tkm
or eye* with p'unty of v.ater; for cye>,
get medical o Men* ion.
C-97
72221
5lbs.
(2.26 ky.)
LOT
714698
Calcium
Hydroxide
For laboratory and
manufacturing use only,
not for drug use.
FISHER SCIENTIFIC COMPANY
Chemical Manufacturing Division
Fair Lawn, New Jersey
Made in U.S.A.
Figure 13- Typical chemical packaging label.
57
-------
3*2_._3_.fr Record easily visible phys_Icajproperties - Observation of the
following properties of the spilled material can confirm an identification or
possibly identify the specific chemical involved (5). However, the MOS must
approach the spill cautiously and not endanger himself and others in deter-
mining the characteristics. If a certain physical property cannot be readily
identified, do not answer that question and go on to the next one.
1. What state is the spill: 1. Solid (powder, pellet, granular)
2. Liquid
3. Gas
2. Is there a noticeable odor from a safe distance?
Pleasant - almond, ammonia, benzene, fragrant, lysol.vinegar,
sweet
Unpleasant - sulfur, irritant, foul, skunk, onion, sharp,
biting, mothball, cleaning fluid, paint
3. What color is it?
1». Is it turbid?
Opaque
Clear
Cloudy
Other
5. If it is in water, does it
6. Does it cause your eyes to water?
7. Is it
float
sink
mix (soluble)
remain unmixed
Yes
No
fuming
flaming
foaming
or is a gas being given off
or is another noticeable reaction occurring
3.2.3.5 Contact the OSC - Once this information has been assembled, the OSC
should be contacted. The information can be transmitted to the OSC who will
then direct the MOS to perform additional steps to aid in identification or
will direct him to begin to assess the danger potential of the situation.
3.2.3.6 Further steps for identification - If so directed by the OSC the MOS
can take one or more of the following steps to aid in specific identification
of the spilled material:
1.
Make on-site inspections to determine which cargo is damaged
and undamaged:
58
-------
This procedure requires the MOS to be very cautious and board
the vehicle to check the cargo. The procedure is only required
for mixed loads and will allow elimination of various cargoes
which have not been damaged from the list of possible materials
involved in the spill.
2. Take samples for chemical testing: The OSC may direct the MOS
to collect samples and then ship or deliver these samples to
a specified laboratory. Care must be taken at all times to
protect the MOS. The spill should not be approached without
fully protective clothing.
3.2.A Assessment of Spj 1 MtegjiJjiujJe arid Human Danger Potential by the_ MJDS
3.2.4^1. General - Once the spill has been identified as to its specific
constituents, the magnitude of the spill and its potential danger to human
safety must be established. To determine this, the MOS must answer a series
of questions which pertain to the spill situation. The OSC can then establish
the effect of the spill using various references.
3.2.^.2 Magnitude of the spill - The MOS can gather the needed information
regarding the spill to give to the OSC by answering the following questions:
1. Note the label information, if available.
2. What type and size of individual containers have spilled the
material?
1. Metal drums aoprox. height
diameter
2. Fiber drums approx. height
diameter
3.
k.
5.
6.
7.
Bags
Paper
Polyethylene
Cyl inders
Carboys Di
Boxes Type
Other
Length
Lenqth
Length
ameter
Length
Dimensions
Width
Width
Width
Height
Width
Height
Height
Height
Heiqht
3. How many of each type of container have been spilled?
k. If large tank trucks or cars or barge and ship holds are
involved, the approximate size can be estimated by pacing off
-------
a similar distance at a remote location.
Size X ._ X
Often the tank cars" and trains are labeled" so the capacity
should be recorded
3.2.^.3 Human Da_n£er_ PotentJ_aJ_ - Information regarding environmental con-
ditions and location oT the spill is necessary to determine the danger which
exists from the spill itself. There are various questions which must be
answered by the MOS and then this information transferred to the OSC.
1. What time did the discharge start,
Determine this information by questioning eyewitnesses to
the spi11.
2. Where is the discharge occurring? (!e. location of spill)
The same information is required as was indicated in the
identification section. Necessary information for each
spill source is summarized in Table 9-
Table 9. METHODS OF IDENTIFYING SPILL LOCATION
Transportation Mode Method
Train Railroad track owner/nearest town (name
and distance) railroad track milepost
(alternate as for trucks)
Truck Highway name/highway number/nearest town
(name and distance)/distance from road
Bus Same as for truck
Airplane Distance and direction from highway/location
on highway as for truck
Ship Name of waterway/nearest coastline/distance
and direction from shore/location & name
of nearest town
Barge Same as for ship
Pipeline Pipeline marker or distance and direction
from highway/location on highway as for
truck
Storage Tank Address in relation to nearby streets, dis-
tance and direction from highway/location
on highway as for truck.
3. How close is the spill to populated areas?
*». What is the spill affecting?
a. ITI water
-------
b. On land
c. In ai r
d. Combination (indicate which)
5. Are any water intakes or wells in the near vicinity?
6. What is the rate of discharge?
7- This rate can be estimated by noting indirect factors
including:
a. What is the shape or type of hole or leak?
Triangular hole
Rectangular hole
Split seam
Valve leak
Puncture
Breakage ^
b. How high is the liquid above hole/water?
(If !n water)
c. Is the hull listing? (Ship or barge)
d. How much material is left in the tank?
(Approximately 1/2, 1A, etc.)
e. If the source of the spill can be safely approached, the
rate can be estimated by measuring depth differences and
the area of the tank measured as follows: (6)
1. Determine the length and width
of the leaking tank. length width
2. Stick a long, straight pole
(gage pole) or "dipstick" down
into the tank either through an
"ullage" hole, or through a hatch
cover, pull it up, note what time it
is, and measure the length of the
pole which is "wet". time (1) length(l)_
3. Wait 15 minutes or so if the leak
is slow, or a shorter period of
time if it is relatively fast. time (2)
*4. Repeat step 2 above. length (2)
If stopped, how long did the discharge last?
61
-------
8. How much area is affected by the spill?
Land: Pace off the length and width of the affected area
from a remote similar distance and record.
length
wi dth
Water: a. Indicate the type of water body affected.
Ocean / River / Lake / Bay / Harbor / Stream / Swamp
(Other)
b. Estimate the size of the water body. Pace
off the affected distances from shore or use
Figure M to estimate stream width.
Stream
Width (feet)
0-75
75-200
200-i»00
1*00-800
800-1200
ft x 0.305 - m
Figure }k Estimating
Stream
Width (feet)
1200-1800
1800-2200
2200-2800 i
2800-31400 1
greater than 3^00
Stream Widths (6)
Estimate the flow rate if any.
Use the following procedure:
1. Measure a straight distance along length of
water body, length _
2. Drop floating object into water and record
time time (i_) _
3. Record time when object reaches end of
measured length time (2) _ _
J|. Current speed in ft/sec (ft/sec x 0.305 = m/sec)
0 8
["-
[t
length (ft)
.1
)J
. .
ime 2 - time 1 (sec)
Estimate direction of flow (N., S., E., W. , etc.)
Estimate depth of waterway.
If accessible use a stick plunged straight into
the bottom and measure wet level as a depth.
Measure 5n the middle of a stream if possible.
62
-------
If direct measurement is impossible, use topo-
graphical maps of the area to establish depths.
Estimate depth of water near point of
discharge.
The stick technique is best, if access is possible.
If not, choose a similar configuration upstream
of the spill and measure that depth.
If a gas spill is occurring:
a. What is the approximate diameter of the
hole in the cylinder?
b. Is a vapor cloud visible? Yes
No
c. If yes, is the cloud rising
lying on ground
other
9. Is a pool of liquid visible on land or on the water?
10. Where is the leak originating?
Barge Type
Ship Type
Tank Truck Type
Train Tank Car
Ai rplane Hul I
Individual container Type
Pipeline Diameter
Storage tank Diameter Height
11. What is the condition of the source?
Repairable leak
Uncontrollable leak
Eas ily moved
Unmovable
Other
_3_.2.4.fr Meteorological Conditions - Information regarding the
weather conditions is also important in assessing the potential
danger of a spill. The MOS can also answer the following guestions:
1. What is the wind speed and direction? The wind speed can
be estimated using the Beaufort scale. (Figure 15)
The wind direction is that direction from which the wind
is blowing and observation of a lightweight object will
give this information.
63
-------
Wind Speed
Beau-
fort
number Knots mph
0 under I under 1
1 1-3 1-3
2 4-b 4-7
3 7-10 £-12
4 11-16 13-18
i 17-21 19-24
b 22-2? 23-31
7 2U-33 32-3G
t 34-1)0 39-4G
9 41-4? 47-5,4
10 4o-^5 i>l>-03
11 I)b-u3 64-72
llydrog raph I c Uffice
Term and
height of
waves, in feet
Calm, 0
Smooth, less
than 1
Slight, 1-3
Moderate, 3-5
Rough, 5-8
Very rough,
b-12
High, 12-20
Very high.
20-40
Mounta i nous ,
40 and
h fgher
1 n ternat ional
Term and
height of
waves , i n feet
Ca 1m, g iassy , 0
Rippled, 0-1
Smooth, 1-2
Slight, 2-4
Moderate, 4-8
Rough, 8-13
Very rough.
13-20
High, 20-30
Very high,
30-45
Estimating Wind Speed
E f_f t; c j. si o b > e r y eci a t J>gj^ ___
See 1i ke mi rror
Ripples with appearance of scales,
no foam crests
Sm«: 11 wave lets; crests of glassy
appearance, not b' eak i og
Large wavelets; crests begin to
break; scattered wh i tecaps.
SmaII waves, becoming longer;
numerous whItecaps-
rloderate waves, taking longer
form; many whitecaps; some
spray.
t_arger waves forming; whi tecaps
everywhere; more spray.
See heaps up; white foam from
breaking waves begins to be
blown i n streaks,
Moderately high waves of greater
length; edyes of crests beg in to
break into spindrift; foam is
blown in well marked streaks.
High waves, sea bet; ins to roll;
dense st reaks to foam; spray
may reduce visibility.
Very high waves with overhang-
in; crests; sea takes white ap-
pearance as foan is blown in
v^r^ dense streaks; rol1iny is
k»»avy and visibility reduced.
Exceptionally high waves; sea
covered with white foam
patches; visibility st M 1 more
reduced.
Effects observed on I anj_^_
Calm: smoke rises vertically
Smoke drift indicates wind direc-
tion; vanes do not move.
Wind felt on face; leaves rustle;
vanes beg in to move.
Leaves, smaI 1 twigs in constant
not ion; light f lags extended.
Dust , 1 eaves r and loose paper
raised Jp; small branches move
Small trees in leaf b« ., \ n to sway.
Larger branches of trees in mo-
tion, whistling heard in wires.
Whole trees in motion, resistance
felt in walking against wind.
Twigs and smalI branches broken
off trees; progress generally im-
peded ,
Slight structural damage occurs;
state blown from roofs.
Seldom experienced on land;
trees broken or uprooted; con-
s ideralbe structural damage
occurs.
Very rarely expertenced on land;
usually accompanied by/ wide-
spread Jamage
Knots x 1.185 - km/hr
mph x 1.61 « km/hr
ft x 0.305
Figure 15. Beaufort scale for wind speed estimation.
-------
2. What are the weather conditions?
ie. Temperature of air
humidity of air
percentage of sky which is cloudy
weather conditions "
rainy
snowy
dry
humid
This information can be obtained by direct observation and
the weather bureau reports.
What is the weather forecast?
This information is important especially when precipitation
is expected and it can be determined from weather bureau
reports.
Weather forecast
3.3 DIRECTIONS FOR THE OSC
3.3.1 Assumptions
There are two assumptions basic to this section regarding the OSC:
1. The OSC has experience in handling a spill situation and will
give immediate information or instructions over the phone
2k hours/day.
2. The OSC has many spill response references available
including those listed in Table 8.
In addition, the OSC will have direct access to other refer-
ence material at the Regional Response Center.
3.3.2 Identification
3.3.2.1 General - The OSC will use the information relayed to him
from the MOS and apply his experience and resources to establish a
positive identification of the material involved. This Identification
process may require only one or two steps plus confirming identifi-
cation by physical properties or it may require lengthy phone calls
and searches. The following paragraphs discuss the possible pro-
cedures which can be followed.
3.3.2.2 Step 1 - Collect Information From MOS - The OSC first must
assimilate the MOS information. The answer is placed on sheets
identical to those the MOS has completed, Sections 3.2.3.2-3.2.3.^.
-------
Then the OSC can begin to use the information.
3.3.2.3. Step 2 - Identification From Shipping Papers - If papers are
available with the vehicle, the process of identification is as follows:
Determine if a multiple or single load is involved.
a, If a single load is being shipped, the identiflest?P^ Is almost complete
but the shipping company should be contacted for confirmation.
b. If multiple loads are involved, a further study is needed. First, study
the list of materials from the freight bill and then investigate the
following possibilities.
1. Is an extremely posisonous gas involved?
2. Is a flammable or explosive material involved?
3. Are incompatible chemicals on the same vehicle? (See Table 10)
However, the chart should not be used as an infallible guide. It should
only provide general guidelines regarding chemical incompatibility. An
expert should be consulted regarding any known mixture and the potential
compatibility confirmed.
If the situation is not safe for a close investigation, the OSC must require
identification by physical properties or sampling. (See Section 3.2.3.6.)
However, if the MOS can enter the vehicle and check the cargo for damaged and
undamaged containers, this should be done. Then the specific hazard may be
identified.
However, if shipping papers are not available or are not available in readable
form, the OSC must obtain a copy of the papers or expert advice regarding the
information. Table 11 summarizes the knowledge necessary for obtaining copies
of the material involved. The reference will indicate telephone number of the
shipping company and the Vice President in charge of operations must be con-
tacted. If it is not working hours, the police in that city may be able to
contact the person needed.
Usually copies are available at the origin of the shipment with the manu-
facturer and possibly with the company receiving the material. The copy at
the shipment origin (ie. loading location) is generally the easiest to obtain,
3.3.2.^ Step 3 - Identification Using Placards and Labels - If the
shipping papers are not immediately available, labels and' placards can
be used to indicate the hazard involved. Extreme caution must be used and
care should be taken to insure that correct information has been gathered.
The two general types of information are available as warning placards or
labels and specific identification labels.
66
-------
TABLE 10. COMPATIBILITY CHART TAKEN FROM CHRIS CG-M6H (8)
CTv
1
2
3
4
5
6
7
8
g
10
11
12
13
14
15
16
17
13
19
20
21
22
23
24
Inorganic Acids
Organic Acids,
Caustics
Amines & Alkanolamines
Halogenated Compounds
Alcohols, Glycols & Glycol Ethers
Aldehydes
Ketones
Saturated Hydrocarbons
Aromatic Hydrocarbons
Olefins
Petroleum Oils
Esters
Monomers & Polymerizable Esters
Phenols
- Alkylene Oxides
Cyanohydrins
Nitriles
Ammonia
Halogens
Ethers
Phosphorus, Elemental
Sulfur, Molten
Acid Anhydrides
1
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
X
2
X
X
X
X
X
X
X
X
X
3
X
X
X
X
X
X
X
X
X
X
X
X
4
X
X
X
X
X
X
X'
X
X
X
5
X
X
X
X Represents unsafe combinations.
The following pages list the chemicals by chemical name and-by
reactivity groups. Obtain the group for the chemical and then
read chart, first from left to right, then down.
6
X
X
X
X
X
'7
X
X
X
X
X
X
X
8
X
X
9
X
X
10
X
X
11
X
X
12
X
X
13
X
X
14
X
X
X
X
X
X
15
X
X
X
C
b
2
t
b
1
b
K
V
1
16
X
X
X
X
X
Chemicals Not On Chart
'•arbon Bisulfide forms an unsafe com-
ination with reactivity groups 1, 4, 19,
0, and epichlorohydrin.
-pichlorohydrin forms an unsafe com-
ination-with reactivity groups 1, 2, 3, 4,
4, 15, 19, 20, 22, 23, 24, and carbon
isulf de.
totor Fuel antikn
nsafe combinatio
4567 15 1
17
X
X
18
19
X 20
X
X
X X
ock compounds form
ns with reactivity groups
9, and 20.
21
22
X 23
~24\
-------
TADLE 10. (continued)
Procedure for use of compatibility chart (8)
I. Determine the reactivity of the product by reference to CHRIS (CG-4^6-1)
2. tnter the Chart with the reactivity group. Proceed across the page. An
"X" indicates a reactivity group which forms an unsafe combination with
the product in question
3. At the end of the line, proceed downard. An "X" again indicates groups
that form unsafe combinations.
'.EMflMBER that this chart is only a guide, further confirmation should be
obtained before assuming the condition is safe. See CG-AA6-I, A Condensed
Guide to Chemical Hazards, page 7~1 to 7-14 for additional information.
68
-------
Table 11. SUMMARY ON HOW TO OBTAIN SHIPPING PAPER COPIES
Type of Vehicle
Truck
Train
Bus
Ships
Barges
Ai rplane
Informatton required
Cab number
Trailer number
Name trucking company
Location and time of
truck spi11
Car number
Name of ra i i road
(from engine or caboose)
Bus number
Name of bus company
Location and time of
bus spi11
Signal flag
Vessel name and number
Location and time of
ship spill
Barge name and number
Location and time of
spill
Airplane number and
name (If any)
Airlines
Location and time of
spill
Reference
Official Motor
Freight Directory
Official
RaiIway Guide
Cal1 Bus Company
(Yellow Pages)
Merchant Vessels of
the U.S.
U.S. Army Corp of
Engineers Ship I.D.
book
Call nearest Harbor
or Port Commission
for reference
Nearest Airport and
the name of the air-
lines
69
-------
The placards are usually general and indicate only hazards rather than
specific identities. The materials which require these placards are
listed in DOT regulations *»9CFR and identities can be confirmed using
this cross reference. However, mixtures or small amounts of materials
are not clearly placarded and, therefore, the lack of a placard or
a "dangerous" warning may be misleading.
Labels are of two types: warning and identification. The required
warning labels are also listed In DOT ^9CFR (2) and the types are
shown in Figure 16. As with placards, the information Is of a
general nature and does not specifically identify the chemical. ^ On
the other hand, individual chemical labels (See Figure 13) provide
specific information and identity of the chemical involved.
To determine information from labels, the OSC must direct the MOS
to closely examine the cargo if this action can be safely accomplished.
The information, carefully recorded, can then be relayed to the OSC
for identification.
3.3.2.5 Step k - Identification Using Miscellaneous Aides - In addi-
tion to the shipping papers and placards, other information is a 1 so
available. One of the most helpful are the Chemcards recommended and
produced by the Manufacturing Chemists Association. The information
on the Chemcards includes (9):
Identification of the cargo
Appearance and odor
Statement of hazards involved and instructions for safe
handling and, as applicable, the need for special cargo
envf ronments
Emergency procedures and precautions
Fire fighting procedures and precautions
However, if mixed loads of hazardous materials are involved, further
identification steps are necessary.
Another aid to the OSC is a requirement by the Coast Guard that all
foreign vessels carrying hazardous materials register the intended
route of the ship with the nearest Captain of the Port Coast Guard
Office. Also, all vessels carrying any of the 40 specified dangerous
cargoes (See Table 12) must notify the Captain of the Port at least
2k hours prior to arrival. Therefore, when ships are the source of
a spill, more detailed information can be obtained from the Coast
Guard.
3.3.2.6 Step 5 " Identification Through Physical Properties - If
there is no direct information available from shipping papers or
other sources, the physical properties can aid in establishing the
identity of the material involved. These properties are also
70
-------
RADIOACTIVE MATERIALS
DM
CLASS 7
CORROSIVE MATERIAL
SPONTANEOUSLY
COMBUSTIBLE MATERIAL
WATER-REACTIVE
MATERIAL
HOIt Moy &• «n*d ki
addition la alh«
BUNG
EMPTY
CAUTION
Do not unKT«w OTtirvIv until •*•
factor pnmurt torn neaped rtwoujyi tfw
hwtarwd tfinxk.
MEMOVE BUNG IN OPEN AIR. KMP
•fl op«n ftwna l^ts •od Ant •«•?.
CndOMd Ei«ctrie Ujhci wt »f«.
NON-DOT LABELS USED FOR AIR SHIPMENTS
CARGO I
AIRCRAFT !
ONIY l
DAM6EH PtLIGRC
-,, ^...-.r'-Jill MAGNETIC S\ x,
-J 14ATCDIAI X-^*X
MAT6BIM
REQUIREMENTS;
1. The above DOT labels are
authorized for immediate
use.
2. Previsouly required labels
may be used until the dates
indicated below at which
time the above labels become
mandatory.
Explosive labels - Jan. I, 1971*.
All other labels - Jan. 1, 1975.
(continued)
Figure 16. Hazardous materials warning labels.
71
-------
EXPLOSIVES
ClASSA
CtASSB
COMPRESSED GASES
*L X
OXIDIZING MATERIAL
FLAMMABLE LIQUID
CIASS3
FLAMMABLE SOLID
-------
Table 12. HAZARDOUS CHEMICALS DESIGNATED BY THE COAST GUARD
Acetaldehyde
Acetone cyanohydrin
Aceton Itri1e
Ac ry 1 on 11 r 11 e
Allyl alcohol
Allyl chloride
Ammonia, anhydrous
Aniline
Butadiene
Carbolic acid
Carbon dtsulfide
Chlorine
Chlorohydrins, crude
Crotonaldehyde
1,2 dichloropropane
Dtchloropropane
Epichlorohydrin
Ethylene
Ethyl ether
Ethylene oxide
Hydrochloric acid
Methane
Methyl acrylate
Methyl bromide
Methyl chloride
Methyl methacrylate (Monomer)
Nonyl phenol
Oleum
Phenol
Phosphorus, elemental
Propane
Propylene
Propylene oxide
Sulfuric acid
Sulfuric acid, spent
Tetraethyl lead
Tetraethyl lead mixtures
Vinyl acetate
Vinyl chloride
Vinyltdene chloride
useful in confirmation of the identity of the spill. The specific
properties required are outlined in Section 3.£.3./». Once these
properties are recorded, then OHMTADS (10) can be contacted to run
a computer search for chemical identity. This source can be easily
referenced and the Information obtained as soon as possible. Another
way to utilize the information is through the EPA publication
"Field Detection and Assessment Manual for Oil and Hazardous Material
Spills" (5). The physical properties of many chemicals are listed in
this manual and eliminations can be done to establish the identity
or eliminate non-spilled chemicals.
3.3.2.7 Step 6 - Identification Through Sampling and Analysis -
The finaltype of identification is done by sampling the spill in the
contaminated area and then analyzing to determine the specific
chemical involved. The simplest approach is to indicate to the
laboratory performing the analysis what the possible contaminants are.
This information can be established from shipping papers, warning
labels or physical property Identification.
The OSC must contact a qualified analytical laboratory and then relay
their specifications to the MOS for sampling. It is important that
the sample be delivered to the laboratory as soon as possible to
hasten identification of the chemical. Therefore, a laboratory in
close proximity to the spill is desirable.
73
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3.3.3 Assessment
3.3.3.1 General - Once the Identity of the chemical spilled is known,
the assessment of spill magnitude and human danger potential must be
established. This process requires utilization of the input from the
MOS into prepared programs to assess the danger involved. The OSC will
need to contact the CHRIS system and access the HACS computer.
This procedure, however, does require both knowledge of the CHRIS
system and gathering of necessary input data.
3.3.3.2 Assessment of Human Danger - The most comprehensive resource
available is the CHRIS Hazard Assessment Handbook, CG-M6-3, the
third volume in the four volume set of CHRIS manuals. This
handbook and HACS, the associated computer program, can provide
extensive information for many types of spill situations. Some of
the computer outputs are listed in Table 13. Determination of the
appropriate program to use is directly related to the identity of the
chemical spill. The second CHRIS manual lists a hazard assessment
code for which various calculation procedures can be followed to
determine the extent of the hazard involved. This procedure is shown
schematically in the Hazard Assessment tree shown in Figure 17.
The geometric shape of the outlined information indicates the type of
input required. The oval shapes are indicative of physical properties
of the chemical, the triangles indicate the environmental conditions
at the spill site, and the rectangles represent the information calculated
by the program. Various inputs are required in order to establish the
hazard potential. For example, CHRIS requires inputs of primary and
secondary information to directly assess the effect of the hazard
(See Figure 18). This information is gathered by the MOS and must
be transformed into an acceptable form for the HACS or CHRIS input.
3_.3.3.3 Hagnitude of the Spi 11 - Prior to the use of CHRIS or any
other reference, the size of the spill must be determined. There
are various ways to establish this information including:
a. Approximate size and description of packages damaged.
b. Determine number of damaged packages.
c. Estimate amount of material released«
(eg. 1/2, 1A, etc.)
d. Confirm package size and volume estimates from Table H
and 15 and the data found in the DOT regulations on
hazardous materials which regulates amount of material
per package. (3)
-------
TABLE 13. CALCULATIONS AVAILABLE IN CHRIS HAZARD
ASSESSMENT
Gases (Tdxic or Flammable)
Flame Length
Flame Angle
Safe Distances
a. For People
b. For people with protective clothing
c. For wooden buildings
Travel Time of Gas Cloud
Duration of Hazard
Liquids
Flammable
Pool size
Flame length
Safe d i stances
For people
For people with protective clothing
For wooden buildings
Water Pollution
Human toxic levels
Concentration of water at downstream location
Time of arrival at downstream location
Maximum distance hazardous to humans
Volatility Hazard
Maximum downwind extent of flammability hazard
Maximum half-width of flammability hazard
Maximum downwind extent of toxic hazard
Maximum half-width of toxic hazard
Maximum duration of flammability hazard
Maximum duration of toxic hazard
Solids
Reactive Sol ids
Amount of projected reaction products
Specific hazard as related to product type
Soluble (same calculations as liquid)
75
-------
\*ccice*jr~\
1 - A. ' I *MrC or XELTAZE I
/4 O \ttt»Hfirr tetfjsec I
Figure 17. Hazard Assessment Computer System (HACS) Hazard Assessment Tree (6).
-------
PRIMARY INFORMATION
I. NAME of chemical
2. TIME discharge began
3- WHERE discharge occurred
4. HOW MUCH was originally present
5. WIND speed and direction _
b. CLOUD cover
7- CURRENT speed and direction
8. WIDTH and DEPTH of waterway
9. HOLE DIAMETER (if gas)
SECONDARY INFORMATION
1. a) RATE OF RELEASE if still leaking
b) TIME TO EMPTY TANK if discharge stopped
c) AMOUNT LEFT in tank
d) SIZE, SHAPE of HOLD
e) LENGTH, WIDTH, SHAPE of TANK
f) HEIGHT OF LIQUID ABOVE HOLE/WATER
2. WATER TEMPERATURE
3. DEPTH of water near discharge
k. WIDTH if river or channel
5. POOL SIZE if visible
6. ACTION ON RELEASE
7. a) VAPOR CLOUD VISIBLE?
b) If yes, RISING OR LYING LOW
8. CONDITION OF VESSEL
9. TYPE, SIZE OF VESSEL
Figure 18. Information needs for CG-M6-3 summary (6)
77
-------
TABLE 14. USABLE VOLUME OF SHIPPING CONTAINERS (11)
Container size 5 description
Usable volume,
METAL DRUMS
55 gal. steel std., 18 gage plate, DOT-17E, new
55 gal. steel std., 16 gage plate, DOT-17C, new
55 gal. steel, removable head, 18 gage, Rule 40, new
55 gal. steel, removable head, 18/16 gage, OOT-17H, new
55 gal. steel, removable head, 18 gage, used, reconditioned
55 gal. steel, std., 18 gage, used, inspected, cleaned
55 gal. aluminum, std., 0.102 in. plate
55 gal. type 304 stainless steel, std., 16 gage, DOT-5C
30 gal. steel, std., 20 gage, DOT-17E
30 gal. steel, removable head, 20-gage, Rule 40
16 gal. steel, removable lug cover, 22 gage
55 gal. steel -mf 11 galvanized, std., 18 gage, DOT-17E
55 gal. steel, removable head, 40-ml 1 polyethylene liner,
external fittings, 20/18 gage, 53.5 gal. usable volume,
DOT-37M
FIBER DRUMS
61 gal., 9 ply, 400 Ib load limit, dry products only, Rule 40
55 gal., 9 ply, 400 Ib load limit, dry products only, Rule 40
47 gal., 9 ply, 400 Ib load limit, dry products only, Rule 40
41 gal., 9 ply, 400 Ib load limit, dry products only, Rule 40
30 gal. 9 ply, 400 Ib load limit, dry products only, Rule 40
30 gal. 7 ply. 225 Ib load limit, dry products only, Rule 40
15 gal. 6 ply, 150 Ib load limit, dry products only, Rule 40
55 gal. 9 ply, polyethylene barrier, 400 Ib load limit,
Rule 40
55 gal. 9 ply, polyethylene-aluminum foil liner, 400 Ib
load limit, Rule 40
55 gal. 10 ply blow-molded 15 mil polyethylene liquid-
tight liner, tight head, steel cover with 2 3/4" NPT
openings, 600 Ib load limit, DOT-21C.2ICP liquid products
30 gal. 9 ply, same as preceding except 450 Ib load limit
30 gal. 8 ply. 300 Ib load limit, removable fiber cover
no barrier
15 gal. 6 ply. same as preceding except 150 Ib load limit
i gal. 5 ply, same as preceding except 150 Ib load limit
55 gal. 9 ply, 400 Ib load limit, semisquare removable
fiber cover, "Rocon" style
45 gal., same as preceding
cu m
0.205
0.205
0.205
0.205
0.205
0.205
0.205
0.205
0.112
0.112
0.059
0.205
0.201
0.228
0,205
0.175
0.153
0.112
0.112
0.056
0 .205
0.205
0.205
0.112
0.112
0.056
0.003
0.205
0.168
cu Tt
7.35
7.35
7.35
7.35
7.35
7.35
7.35
7.35
4.00
4.00
2.14
7.35
7.20
8.15
7.35
6.23
5.48
4.00
4.00
2.00
7.35
7.35
7.35
4.00
4.00
2.00
0.1335
7.35
6.01
continued
78
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TABLE 14 (continued)
BAGS. MULTIWALL PAPER. POLYETHYLENE (PE) FILM Usable volume
Pasted-valve bag, 20 1/2 x 22-in. face, 5 1/2-in. top and ^J-^ cu ^ *
bottom with 1-mil free film, 2/50, 1/60 kraft, plain, no
printing, PE internal sleeve 0.037 (1-33)
Sewn-valve bag, 15 x 5 1/2 x 30 I/A in. 5 1/2-in. PE internal
sleeve with 1-mil free film, 2/50. 1/60 kraft, plain,
no printing 0.0037 (1-33)
Pasted-valve bag, 18 1/2 x 22 3/4 in., 3 1/2-in. top and
botton, PE internal sleeve, 3/50 kraft, plain, no printing 0.023 (0.84)
Sewn open-mouth bag, 20 x 4 x 30 3/4 in., 3/50, 1/60 kraft,
plain 0.056 (2.00)
Sewn-valve bag, 19 x 5 x 33 1/2 in., 5 1/2-in. tuck-in sleeve,
3/50, 1/60 kraft, plain 0.056 (2.00)
Pasted-valve bag, 24 x 25 1/4 in., 5 1/2-in. top and bottom,
tuck-in sleeve, 3/50, 1/60 kraft, plain 0.056 (2.00)
Pasted open-mouth baler bags, 22 x 24 in., 6-in. bottom,
1/130 kraft (or 2/70), plain
Flat-tube, open-mouth bag, 10-mi1 PE film, plain, 20 1/2 x
34 1/4 in. 0.037 (1.33)
Square - end valve bag, 20 1/2 x 22-in. face, 5 1/2-in.
top and bottom, 10-mi1 PE film, plain 0.037 (1-33)
SMALL BAGS. POUCHES, FOLDING BOXES
Pouch, 8 3/4 x 16 3/4 in., 2-ply PE film. 2-ml thickness/ply 0.003 (0.12)
Bag, sugar-pocket style, 6x2 3/4 x 16 3/4 in., 2- to 40-lb.
basis weight, natural kraft paper 0.003 (0.12)
Bag, pinch style, 8 3/4 x 3 x 21 in., 2- to 40-lb. basis
weight, natural kraft 0.003 (0.12)
Folding box, 5x1x8 in., reverse-tuck design, 12-point
kraft board with bleached white exterior 0.0008 (0.028)
Folding box, 91/2x4 1/2 x 15 in., full overlap top and
bottom, 30-point chip board with bleached white exterior 0.01 (0.37)
CORRUGATED CARTONS, BULK BOXES
Regular slotted carton (RSC), 24 x 16 x 6 in., 275-lb. test
double wall, stapled (stiched) joint
RSC, 16 x 6 x 24 in., 275-lb. test double wall, stitched
joint, end-opening style
continued
79
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TABLE 14 (continued)
Bag-in-box, RSC, 15 x 15 x 22 in. 275"1b. test double 0.08 (2.86)
wall, stitched liner, 600-lb. test
Bulk box 200/600 (test in Ib. for both pieces), laminated 0.14 (5.00)
inner lining approximately 41 x 34x 36 in., less PE
1iner and pal let
CARBOYS. PLASTIC DRUMS, JARS. BOTTLES
Carboy, 13 1/2 gal., polyethylene, blow-molded 0.037 (1-35)
Drum, polyethylene, 15 gal., blow-molded, ICC-34 (DOT-34) 0.056 (2.00)
Carboy. 15 gal., glass, nitric acid service, wooden crate 0.056 (2.00)
Jug, 1 gal., glass, with finger handle, plastic cap 0.003 (0.1335)
Bottle, 1 qt. glass, "Boston" round, plastic cap 0.0009 (0.03*0
Jar, 1 qt., glass, wide mouth, plastic cap 0.0009 (0.034)
Jar, 1 gal., polyethylene, wide mouth, plastic cap 0.0037 (0.1335)
Bottle, 1 gal. polyethylene, narrow neck, plastic cap 0.0037 (0.1335)
Bottle, 1 qt. polyethylene, wide mouth, plastic cap 0.0009 (0.034)
Jar, 1 pt. polyethylene, wide mouth, plastic cap 0.0004 (0.017)
CANS, PAILS
Pail, 5 gal., steel, tight head, 26-gage black steel, PE 0.0187 (0.67)
pour spout, unlined
Pail, 5 gal., 26-gage black steel, removable head, unlined, 0.0187 (0.67)
lug cover, wire bail handle
Can, 1 gal., friction wedge lid, handle (paint can) 0.0037 (0.1335)
Can, 1 qt. friction wedge led (paint can) 0.0037 (0.034)
Can 1 gal. oblong "F" style, handle, screw cap 0.0037 (0.1335)
Can 1 qt. oblong "F" style, screw cap 0.0037 (0.034)
80
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TABLE 15. TYPICAL CARRIER CAPACITIES
Tank Truck (11) Average 70,000 Ib. Total Wt.
30,000 Ib/for tandem axles
60 ft. In length
Labeled according to capacity
Tank Car (11) Labeled according to capacity
Ship Tankers Size not limited (estimate cubic size)
Barges (12) a. 35 ft. wide x 195 ft. long x 9' draft
b. 52.5 ft. wide x 520 ft. long x IV draft
lo. Containers (11)
per car load
truck or train
Fiber
61 gal
55 oal
47 gal
41 gal
30 gal
15 gal
1 gal
Metal
55 gal
30 gal
16 gal
Drums
. size
. size
. size
. size
. size
. size
. size
Drums
. size
. size
. size
Number/Carload
300
318
424
552
592
1,272
17,365
360
592
1,225
Ibs x 0.454 • kg
ft x 0.305 " m
gal x 3.785
81
-------
8. Width and Depth of
Waterway or Size of Land
Area Affected
9. Hole Diameter (if gas)
The MOS can transfer this information
or the OSC can determine this from maps
available from USGS.
The MOS must estimate this information
from a distance and relay it to the OSC.
SECONDARY INFORMATION (FOR MACS USAGE)
1. a. Rate of Release, if still leaking - Various methods are avail-
able for estimating the rate of the leak.
The MOS can transfer the information to
the OSC who can do the necessary cal-
culations. For ship holds, the rate of
leakage can be estimated If knowledge
of the type of hole, water depth and
list of the ship is known (Figures
19-22). If the source can be
approached, the rate of leak can be
determined by depth differences over
a known amount of time. An example
follows:
Steps
At time 10:30 a.m. a "dipstick" is put down into a
20-foot long by 10-foot wide tank. It is pulled up and
it is noted that % inches of the pole are "wet". At
10:^5 a.m. the procedure is repeated and it is determined
that 72 inches of the pole are "wet".
Step 5:
96" - 72" = 2k"
2V x 1 ft/12" = 2 ft
Step 6:
2 ft x 20 ft x 10 ft
400 cubic it
15 min ~ =
cubic ft
cubic ft
26.66 min
Step 7:
26.66 cub!c ft
mn.
mm
x 3.781.
•
7.*>8 gal.
cubic ft
1
min.
rate of
release
82
-------
b. Time to Empty Tank
(if discharge Is
stopped)
c. Amount left In Tank -
d. Size, Shape of Hold
(!f applicable)
This information can be obtained by the
MOS by eyewitnesses at the scene,
The estimate based on the percent of
material left in the tank is made by
the MOS.
If a hold is involved, the size can be
estimated by the MOS, alternately the
ship's registration papers should
include this information.
Length, width and shape- The MOS should also give this infor-
of tank mat Ion or the best estimates. If
these are not available, the regis-
tration papers of the tank car should
give the Information.
Height of Liquid Above - The height is determined by the MOS
Hole/Water and relayed to the OSC.
2. Water Temperature
3. Depth of Water Near
Discharge
». Width (if river or
channel)
5. Pool Size, if visible
6. Action on Release
7. Vapor Cloud Visibility
and Action
The MOS can establish the temperature
by borrowing a thermometer or possibly
certain agencies may have this
Information available.
This Information can be relayed to
the OSC by the MOS. If an on site
depth measurement is not possible,
a similar upstream location can be
measured.
The MOS can estimate this or the OSC
can use maps of the water body to get
an approximate value.
The MOS must estimate the pool size
and relay the information to the OSC.
Specific action of the chemical on
release must be reported to the OSC.
The existence of a vapor cloud and
Its action regarding low lying or
rising Is needed to be reported by
the MOS.
83
-------
oo
-tr
b, (feet) Deck plow l9Pm) «
, Reference line
_
.25
5-
(
.75
1.0-
—
3 —
4 ~
5 ~
6 -
7 -
8 -
9 ~
10
r- b — | /
Liquid \ / . t
Level ^$%%! 1
Yfr%y h d
V 1 1
( \
Side View of Barge or Ship
* — _
••*••. ^^
-— ,^
(J^"^'
ft x 0.305 " m
gpm x 0.063 " I/sec
10 -
.005 25 '
50 -
- -01 100 .
250 -
500 -
1,000 -
• .05 ^<
^ . 2,500 .
• .1 ***^ 5,000 -
>
-------
.or
.05-'
.25'
.5 - -
1.0 -
2. - -
5.
6.
7.
8.
10. 1
ft
b
b = is the width of the hole
h = is the height of the liquid
level above the bottom of
the hole or the water level,
whichever is higher.
•10
M
-25
.50
-100
-200
-300
•500
-1000
-2500 ^- -^
-5000 ^ ""
'10,000
•25,000
•50,000 :
•100,000 :
-250,000 :
Side View of Barge '
-500,000 or Ship
"1,000,000 t t~b~*l De^kx/
-1,500,000 \
•p nnn nnn ....
HH j '
f)\fj n r-i m A\\\\\\\ 1 O 1 r n
» 9P"i base
(
ieet)
[-1
.2
-3
-4
-5
-6
-7
-8
-9
-10
-11
-12
I13
-15
:•??
:23
'25
Liqu
)
of o|
wate
ft x 0.305 " m
gpm x 0.063 « I/sec
Figure 20. Rate of chemical discharge from a
rectangular slot-shaped opening.(6)
85
-------
A, (sq. ft.) Flow (gpm) SMt
. onn V
.1
.25 •
.50 -
1.0 -
2 .
3
4 -
5
10
15
1 V
20
25 -
ChS
30
40 -
50 •
70 :
100 :
-
.
— b W
250 I
500
1,000 "
- 2,500
J"
5,000
- 10,000
• 25,000 _^_
- 50,000
- 100,000 A "
h -
- 250,000
ft X
- 500,000 gpm x
- 1,000,000
t View of Barge or Ship h y^
\
^®>—*- \
A^*^ >WatPr
' ^ 1 ' "*"
or
) , S Liquid Level
; I h (
( >$? /Water "
) A^^ ) Line
\ /
. .
is the estimated area of the
hole in square feet
is the height of the liquid level
above the center of the hole or
the water line, whichever is higher
0.305 - m
0.063 - I/sec
1
2
3
4
• 5
- 6
- 7
• 8
9
10
11
- 12
: 13
- 15
- 18
' 20
- 25
Figure 21. Chemical discharge from Irregularly shaped holes.(6)
-------
100
Time
Figure 22. Comparative cargo loss versus time for three types of opening (6)
87
-------
3 3 3.A Establishing Inputs for Assessment Calculations - Required
Inputs for the CHRIS manual CG ^6-3 and the MACS computer program
are shown in Figure 18. The MOS will have answered various
questions regarding the spill problems and must relay this infor-
mation to the OSC (Section 3.2.^.3) The OSC can copy the answers,
direct the MOS to further action and then begin compilation of data
to input CHRIS.
PRIMARY INFORMATION (for hand calculations in CHRIS CGM6-3)
1. Name of Chemical
2. Time Discharge began
- The identity will have to be established
by one of the steps outlined in
Section 3-3.2
- The information on the specific dis-
charge time can be determined from
the MOS who has interviewed various on
scene witnesses.
3. Where Discharge Occurred - The specific location of the discharge
is indicated by the MOS in Question 2.
This information is augmented by
Questions 3 and k regarding the proxi-
mity to populated areas and drinking
supplies. The OSC should also consult
maps of the area to pinpoint other
hazards.
How Much Was Originally
Present?
5. Wind Speed and Direction -
6. Cloud Cover
7. Current Speed and
Direction (when appli-
cable)
The information is established from
the size, and number of containers
involved and then confirmed by con-
sulting DOT shipping regulations (3)
The MOS will relay the information from
either Beaufort Chart or Weather Bureau
summaries.
Again, the MOS can relay the percent
of the sky covered with clouds.
The current speed is found using the
following formula.
Current Speed
\sec,/
* 0.8 X distance measured (straight)ft.
time to cover distance (sec)
The direction is given by the MOS or
found on maps. (ft/sec x 0.305 - m/sec)
88
-------
MAXIMUM WIDTH OF THE CLOUD THAT MAY BE HARMFUL
M««nwn Width o)
slo«ic Ckxid-Fw
Olemicil Neine
end Code*
10000
JO.OOO
x.oon
Aceteldehyde AAO
Arranonie. Antiydrout MIA
lutldirne. Inhibited SOI
Btiune BUT
I Tan
BITo™
100 Tom
Chlorine
CLX
I Ton
Dichlorodilluorometntne DCF 53 100*1001
Difnethyljmine
DMA
Ethyl Chloride ECL
Ethylene O«k)e EOX
i Chlonde HOC
Hydrogen Fluandt HFX
LiqulfM Ptlrolfum Gil LPG
Methyl Bromide MT8
Methyl Chloride MTC
MonocMorodilluoromethine
MCF
Nitrogen Tetroxide NOX
rropine f
rropyrene
Sulfur Oioicldt
Vinyl CNo.«h
SFO
10 Tom
3100 To,
\ '/'.\ 100Tom
10 TO™
^lOOToi
1 Ton
10 Tont
i 100 Too,
.10 To".
ItOOTor*
ITon
1 10 toix
>7T< 100 Toi
Figure 23. Effects of Toxic Gases (6)
-------
MAXIMUM DOWNWIND DISTANCE OVER WHICH GASES MAY BE HARMFUL't
"X. Maximum Doomeind
Chemical NamfN.
aid Code** 1 ^v».
t \^0 5 10 15 » 75 30 35 40 «
AatakMiyda AAO
Ammonia. Anltydreui AM
Butadiene. Inhibited BDI
Butane BUT
Chlorine CLX
Dichloiodifluoromtlhane OCF
Dimethyljmine DMA
Ethyl Chloride ECU
Elhytene Oridt EOX
Hydrogen Chloride HOC
Hydrogen Fluoride HFX
Liquefied Petroleum Gai LPG
Methyl Bromide MTB
Methyl Chloride MTC
MonoctilorodilluororrMthene MCF
Piopene PUP
Plopytem M>1
Sulfur DkuUe SFO
Vinyt CMoride VCL
1 iL ' ' ICkmit 0»cr»gJll
^^/A4 lOOTonj
.//jtfi"'s72jt 1OO Tom
''' "" ''s^'ty^y''', ''' ''*'' ' ' •'' - '''"''"'•'.'* -'''S-'S''"
\ 1 Ton
T 10 Tom
S/ss V. 1 10U Tom
r7/T ff'JJ^ 1 Ton
,'/' - s,/S,''f'/f,<'S'' '.''•'//'''
llTon
t _' n ^JJ 100 Tom
^^.•.' .' -< i 10 Tom
1VoV™«
^ll^j '00 Tom
" "/(V- '•' -1 ' '^-V t-'-f'-W$fYfr . . i u 1f
1 Ton
^. '/ '. 1 100 Tom
/TTTt 100 TJ««
V '-••'•• 1 1 T.-n
//. • '• *"-' *JSW ''>.».'. *SS\ 10 Ton, 10
7V£j_«io TU^
' ' ; TTVi''-"-l"t1 '00 Ton*
K) tQU Tom
1 Tom
OTom
Ml IOO Ton*
*He»rd CAtculjlert AMurranQ wot^l c** WNtnet rondit-oni (ile«dy Inw wind) «rnj >n%l«nuti«t>ui diu rMiqe
ISee Teble 5 3 lor tiine ot
-------
EXAMPLE 1
MAXIMUM DOWNSTREAM
HAZARD EXTENT
THIS AREA IS ALSO
CONSIDERED PART
THE HAZARD ZONE '
HAZARD ZONE PREDICTED BY
HAZARD CALCULATION CODE AC
RIVER
WIND DIRECTION
SPILL SITE
FLOW
EXAMPLE 2
MAXIMUM HALF-WIDTH
OF VAPOR CLOUD
MAXIMUM EXTENT OF
HAZARD
AREA WITHIN DASHED
LINES IS CONSIDERED
TO BE HAZARD ZONE
\
RIVER
\_J
DISTANCE DOWNSTREAM
THE CHEMICAL WILL
TRAVEL BEFORE
DISAPPEARING
WIND DIRECTION
SPILL SITF
MAXIMUM HALF-WIDTH
OF VAPOR CLOUD
Ftqure 2k. Wind effect on hazard zone (6).
91
-------
8. Condition of Vessel
or Vehicle
9. Type and Size of Vessel
- This Indicates the stability of the
situation and the possibility for
leak stoppage.
- This information reported by the OSC
pertains mainly to ships at sea.
3.3.3.5 Application of the Assessment Information - The OSC wi 1 1 then
receive output from the HACS computer system indicating the affect of
the hazards on downwind or downstream populations. (See Figures 23~2A)
This information can then be relayed to the Civil Defense Agency or
police department so appropriate action to safeguard the population
can then be taken.
3.3.^ Remedial Action
Various methods of remedial action are appropriate, once the identity
and danger of the spill has been assessed. The remedial action may
involve covering the spill, absorption, chemical addition to change
the pH or other actions. The comments section of the chemical treat-
ment scheme in Chapter 4 indicates some remedial action. CHEMTREC
and other emergency agencies should be consulted regarding other
possible steps to take.
92
-------
IKO-CHAPTER 4 - DETERMINATION OF THE BEST METHOD FOR SPILL HANDLING
4.1 GENERAL
Once the spill has been identified and assessed, the best containment and
handling method must be determined. This chapter presents methods to
allow the user to determine the best techniques for a specific situation.
The chapter covers containment, choosing the best handling method, and
specifics regarding handling techniques including over 300 schemes for
treatment of different hazardous chemicals. The chapter is used in con-
junction with Chapters 5~7 to complete the construction of a treatment sys-
tem if treatment has been selected as the best handling method. The
methods of following Chapter '( and its integration with other chapters is
shown in Figure 25-
4.2 CONTAINMENT OF SPILLED MATERIALS
A.2. I Stepwise Approach to Con_ta ' riment
The following steps should be taken when containment of a spill is necessary:
(a discussion follows)
I- Establish identity. (Chapt&r 3)
2. Establish human safety hazard and take appropriate safety precautions
and/or remedial action. (Chapter 3)
3. Stop discharge whenever possible.
k. Note location of spill
on land
on water
in water
under water
in air
5. Refer to appropriate figure (or figures for combined spills), the
accompanying text, and the appropriate oil spill containnent references,
if necessary.
6. Choose a method of containment which seems best.
7- Evaluate choice by answering the corresponding questions.
8. If all answers lead to containment, proceed taking adequate safety pre-
cautions .
9- If containment by that method is not feasible, choose another possible
technique and evaluate it.
93
-------
Choice
Best Con
tatnment
Method
Chapter 3
Chapter
5
Construction
Figure 25. Use of Chapter k.
-------
10. Continue to evaluate alternatives until a method is established
or no feasible containment method is found.
Steps I & 2 Identification and Assessment ~ Use the procedures outlined
in Chapter 3 to identify and assess the spill. Do not contain the spill
without knowing the identity and hazard potential because the MOS may be
exposed to great danger.
Step 3 Stop Discharge Whenever PojisJ^bjji - To do this the MOS must approach
the spill so adequate safety measures must be taken. Procedures to stop
the discharge are listed below and are only included as possible suggested
methods:
I. Close valves and shut off pumps - especially if a transfer operation
is involved.
2. Rebuild or repair container - includes rebuilding, reinforcing,
patching and insertion of plugs (13) both to the inside (rags to
get caught in the leak) and from the outside (wooden plugs forced
into hole to reduce area of leak).
3-. Change the position of the container - move the container so the
leak is at the highest level.
k. Transfer or collect the material from the leaking container -
usually into an undamaged container of the same or similar type.
5- Encase the entire container or construct a suitable alternate -
either overpacks or actual containment can be done in this circum-
stance (I1*).
The situation must be evaluated and then the MOS must determine if one of
these procedures is applicable, or safe.
Steps 4 & 5 Locate Spill and Refer to Figure Summaries ~ The next step
involves establishing the specific location of the spill, i.e., on land,
in, on or under water, or in air. The spill could be located in a com-
bination of media and this factor must be noted. Then the MOS must refer
to Figures 26-30 which summarize the containment methods for various spills
(15). It must be emphasized that the figures present diagrams to illustrate
the containment technique. Details regarding its implementation are not
included. The MOS must refer to the references listed in Table 16 for the
needed background on containment.
Step 6 Choose Apparent "Best" Containment Method - The choice is made from
knowledge of the type and size of the area affected by the spill, meter-
ological conditions, and the materials available to the MOS. These mater-
ials can either be immediately on hand, which is the best situation, or
can be brought to the scene 5n a short time. Other considerations are
the safety hazard and the toxicity of the material spilled, the proximity
to populated areas or water sources, and the accessibility to the spill
95
-------
TABLE 16. OIL CONTAINMENT REFERENCES
Ayers, R.R., A Rigid Perforated Plate Oil Boom for High Currents, Report No.
EPA 600/2-76-263, National Technical Information Service, Springfield,
Virginia 22161 , 1976.
Bonz, P.E., Fabric Boom Concept for Containment of Floating Oils, Report No.
EPA 670/2-73-069, National Technical Information Service, Springfield,
Virginia 22161 , 1973-
Breslin, M.K., Testing of Boom Configurations for Calm Water Spill Contain-
ment, EPA Report, Oil and Hazardous Materials Spills Branch, U.S. E.P.A.,
EdTsbn, New Jersey 08817, 1977.
Guide to Water Cleanup - Materials and Methods. Arthur D. Little/Learning
Systems, Cambridge, Massachusetts 02140,
McCracken , W.E., Hydrodynamics of Diversionary Booms, EPA Report, Oil and
Hazardous Materials Spills Branch, U.S. E.P.A., Edison, New Jersey 08817,
1977.
McCracken, W.E., Performance Testing of Selected Inland Oil Spill Control
Equipment, Report No. EPA 600/2-77-150 , National Technical Information
Service, Springfield, Virginia 22161, 1977*
McCracken, W.E. and Schwartz, S.H., Performance Testing of Spill Control
Devices on Floatable Hazardous Materials, EPA Report, Oil and Hazardous
Materials Spills Branch, U.S. E.P.A., Edison, New Jersey 08817, 1977-
Proceedings, 1973 Oil Spill Conference, American Petroleum Institute,
2101 L Street, N.W., Washington, D.C. 20037, 1973-
Proceedings, 1975 Oil Spill Conference, American Petroleum Institute,
2101 L Street, N.W., Washington, D.C. 20037, 1975.
Proceedings, 1977 Oil Spill Conference, American Petroleum Institute,
2101 L Street, N.W. , Washington, D.C. 20037, 1977.
Schwartz, S.H., Performance Testing of the Navy Standard Boom and P. A. A. Boom,
EPA Report, Oil and Hazardous Materials Spills Branch, U.S. E.P.A., Edison,
New Jersey 08817, 1977-
96
-------
DIKING
SIOEVIEW
SPILL
n
DIKE
GROUND LEVEL
GROUND
LEVEL
:^ DIKE
SPILL
TOPVIEW
©
ENCIRCLI'ir,
DIKE
SPILL
CONTAINED SPILL
DOWNHILL
DIKF
1. Suitable dike materials must be available, either natural soil,
sand bags or foam.
2. Proper earth moving equipment or specialtzea foam dike equioment
must be obtainable.
3. An advantageous site must be available.
k. This procedure may not eliminate percolation of the spill
through the soi1.
II, EXCAVATIONS
SPILLED MATERIAL
—-=-/ EXCAVATED PIT
1. Equipment and land must be available to accommodate the excavation
2. In certain areas, soil or subsoil nature may render excavation
Impossible or Ineffective.
Figure 26. Containment of spills on land.
97
-------
EXCAVATION AND DIKING
CURRENT
WATER LEVEL
DIKE OF SANDBAG OR MATERIALS FROM
NATURAL SLOPE ^X^P~/^^^ EXCAVATION
CONTAINED SPILL
EXCAVATION
1. Difficulties may be encountered when attempting excavations
under water.
2. Natural forces such as currents or slope of the bottom may be
utilized advantageously.
3. Increased turbidity may hamper the activity of scuba divers.
A. Material needs may include divers, pumps, earthmovlng equipment,
dredges, and diking material.
Figure 27. Containment of spills heavier than water.
-------
I. DIVERSIONS
I
FLOW
UNCONTAMIMATED FLOW -
BARRIER
TO PREVENT
DISPERSION OF
CONTAINED MATERIAL
SHORELINE
EXCAVATION
The equipment and suitable land areas must be available for a large
excavation upon short notice.
2. An effective method of backfilling the excavation must be available.
3. It is possible to use pumps for stream diversion.
FLOW
DIVERSION CHANNEL—-
CAPTURED SPILL
DAM
I. Equipment and suitable land area must be available for a large
excavation upon short notice.
2. An effective method of enclosing the spill with dams must be
avallable.
contInued
Figure 28. Containment of an entire water mass
99
-------
II. GELLING
DIKE TO HELP MOLD
GELLED MATERIAL
\
SIDE STREAM /"• >LLJ .[
GELLED SPILL
MAIN STREAM
I. Gelling Is useful when a limited volume of waste Is to be treated.
2. Treatment and/or disposal of the entire gelled mass is necessary.
3. Application of gelling agents must be implemented a short time after
the spl11 occurs.
l». Trained personnel and specialized equipment must be available.
III. CONTAINING AN ENTIRE WATER BODY
INLET
WATER BODY
CONTAINING SPILL
1. Voluminous overflows may be
difficult to retain.
2. Earthmoving equipment must be obtainable.
DISCHARGE
IKE TO STOP DISCHARGE
EXCAVATION TO CONTAIN
OVERFLOW
3. When more than one overflow originates from a waterbody,
all overflows must be contained.
continued
Figure 28 (continued)
JOO
-------
IV. SEALED BOOHS
TOP VIEWS
ANCHORS
EXAMPLE 1
WATER
LEVEL
ANCHOR LINES
ANCHORS
EXAMPLE 2
SHORELINE
BOOM ANCHORED
AWAY FROM SHORE
SIDE VIEWS
SPILL
-o
BOOM
BOTTOM OF WATERWAY
WATER
LEVEL
SPILL
MOORED TO SHORELINE
BOTTOM
1, The spill must be of limited volume.
2. Wind or current may render this containment method Ineffective.
3. Difficulties In obtaining a sealed boom system may be encountered.
*». This containment method Is applicable In shallow water only due to
bottom seal and anchoring difficulties.
Figure 28 (continued)
ANCHOR
101
-------
I. WE I RS
CONTAINED MATERIAL
WATER LEVEL
- ' _
RIVER BED
1. Weirs may be difficult to deploy properly.
2. Turbulence behind the weir may render this containment method
Ineffective.
3. To be effective the spilled material must be In the upper layer of
water.
II. USING FIREHOSES OR PROPWASH TO DIRECT AND CONTAIN SPILLED MATERIALS
SPILLED MATERIAL-
PROPWASH OR STREAM FROM
FIREHOSES
BOAT SLIP OR FLOODED
DRY DOCK OR BOOMED
AREA
SHORELINE
V
I. Adverse winds or currents may render this method Ineffective.
2. Firehoses or ships must be obtainable, and have access to the spill
site.
3. A suitable containment area must be available.
4. Winds and currents must be taken Into account.
5. Impact water with fire stream at least 6.1-9.2 m (20-30 ft) away
from spl II .
continued
Figure 29. Containment of floating spills
102
-------
III. ENCIRCLING BOOM
CONTAINMENT BOOM
ANCHORS
30.5 - *»5.7 m
(100-150 ft) BETWEEN ANCHORS
1. Heavy seas may render containment with this method Ineffective.
2. Wind or current shifts may render this containment method ineffective.
3. The proper booms and deployment systems may be difficult to obtain.
IV. COLLECTION AND TOWING OF A SPILLED MATERIAL WITH A BOOM
MATERIAL
COLLECTED
BOOM
J TOW VESSEL
SPILLED MATERIAL
TOW VESSEL
TOWING LINES
1. Heavy seas may render containment with this method ineffective.
2. Wind or current shifts may render this containment method Ineffective.
3. The proper booms and deployment systems may be difficult to obtain.
4. Towing speed may be limited to 2.8 km/hr (1.5 knots) or less.
Figure 29 (continued)
103
-------
V. PNEUMATIC BARRIERS
SIDE VIEW
SPILL
TOP VIEW
DIFFUSED
CONFIGURATION
1 '
ENTRAINED WATER
*\",
l',''"—AND BUBBLE CURTAINS-
'—AIR DIFFUSERS
I*
O
1. Wind or current may render this containment method Ineffective.
2. Obtaining proper diffusers and compressors may be difficult.
3. Deep water requires suspension of diffusers In the water column
to increase efficiency of unit.
k. Rarely used.
cont inued
Figure 29 (continued)
-------
VI. DIVERSIONARY AND CONTAINMENT CONFIGURATION
DIRECTION OF WIND OR CURRENT
CONTAINED
SPILL
SHORE
SHORE
1. Whenever possible use with outside bend and sufficient
clearance to reach site.
2. An Intermediate tie is needed to keep "bucket" from
forming.
3. Technique is limited to currents up to 2.^-3.1 mps (8-10 fps)
k. Proper booms and deployment systems may be difficult to obtain.
Figure 29 (continued)
105
-------
VI. DIVERSIONARY AND CONTAINMENT CONFIGURATION
DIRECTION OF
WIND OR CURRENT
BOOMS
30.5 - 45.7
I (100-150 ft.)
UNCONTAINED SPILL
NCHORS
CONTAINED MATERIAL
I. Heavy seas may render this containment method ineffective.
2. Wind or current shifts may render this containment method ineffective.
3. The proper booms and deployment devices may be difficult to obtain.
4. This technique is limited to currents up to 0.3-0.61 mps (1-2 fps).
Figure 29 (continued).
106
-------
I. MISTING TO REMOVE CONTAMINANTS
WATER MIST
AIR SPILL
EXCAVATED
COMTAlNER
AREA
FOR
COLLECTION
1. Not all materials will be removed In this manner.
2. Water source must be available.
3. Require large area for containment of resulting water.
Figure 30. Suppression of air spills
107
-------
location. Specific information on containment methods is presented in
the tables which follow. (Tables 1?-21).
Step 7 Evaluate Choice - Once a preliminary selection has been made, the
choice is evaluated by answering the list of questions (Figures 3I~35)
which are designed to indicate problems with the containment method.
It is important to consider each of the questions individually and deter-
mine if any aspect of containment by that method is limiting. One
question which must be answered regards the hazard effect of containing
the material in a small space rather than allowing natural dispersal
processes to remove it. The specific nature of the material, the size
and type of the area affected, and the mobility of the system will aid
in answering this question.
Step 8 Contain Safely if Indicated - The questions answered in Step 7 wi11
then indicate if the chosen containment technique is feasible. Then the
MOS must proceed cautiously, taking adequate safety precautions to con-
tain the spill. Referral to more specific references regarding contain-
ment is necessary (Table 16).
Steps 9 & I'O Evaluation of Other Alternatives — If evaluation by Step 7
indicates containment by the initial technique is not feasible, other al-
ternatives can then be evaluated to determine the best method of con-
tainment, if any. Once it has been established if the material can or
cannot be contained, then the decision must be made regarding the
succeeding spill handling method.
J*.3 COLLECTION OF SPILLED MATERIALS
After containment, the spill may require collection for containment re-
moval, or treatment. Various methods are available including those
listed. More detailed information is available in other references.
a. Suction Skimmers - Remove surface contaminants by drawing layers
through an orifice. The angle of the orifice establishes the ratio
of water and contaminant to be removed (16).
b. Vacuum Skimmers - Remove floating materials also using a vacuum
tank to generate the drawing force. Useful mostly for small
spills or places where flammable materials are to be removed.
c. Sprbents - Used to collect floating material by distributing ab-
sorbents and then collecting them from the surface of the water body.
d. Dredging - Used to remove insoluble chemicals that are heavier
than water. Various methods are used, however, care must be taken
not to disturb the bottom and create a more hazardous situation (17).
108
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TABLE 17. SPILLS ON LAND
Type
Dikes
Earthen
o
vn
Foamed
Polyurethane
Foamed
Concrete
Excavati on
Excavation
Dikes
Appli cat!on or
Construction Method
Create wi th bul1-
dozer or earth-
moving equipment
to compact earth
(height depends on
earth type)
Use trained per-
sonnel to construct
Use trained per-
sonnel to construct
Bulldozer or earth-
moving equipment -
1 ine if possi ble
Bulldozer or earth-
moving equipment -
1 ine if poss ible
Use
Flat or sloped
surface
Hard, dry sur-
faces
Flat ground
Slow moving spill
Soft ground
Natural cavl-
tatlon
Soft ground
Advantages
1. Hate rial on s i te
2. Construct with
common equipment
3. Construct quickly
1. Hold up to several
feet of water (3)
1. Better adhesion to
substrates (clay/
shale/grass)
1. Material on site
2. Construct with
common equipment
1. Need less space
than separate
2. Material on si te
3. Construct wi th
common equipment
Disadvantages
1. Natural permeability of
soi 1
2. Seepage through ground
3. Surface composition of
sol 1 not sui table in al 1
cases
1. Leaks on wet ground
2. Hard to obtain dispersion
device
1. Hard to obtain foam and
dispersion device
2. Must set for a time period
Will not hold high hy-
draulIc heads (15)
1. Move large amounts of
materi al
2. Natural permeability of
soi 1
3. Surface of soil not suit-
able In all cases
1. Move large amounts of
material
2. Natural permeability of
soi 1
3. Surface of soil not suit-
able in all cases
-------
TABLE 18. SPILLS IN WATER - HEAVIER THAN WATER SPILLS
Technique
Natural Exca-
vations £
Dikes
Construction
of excava-
Applicatlon or
construction
method
none
Dredges: hydraulic
or vacuum pumps
Use
Where a natural
barrier exists
1 f bottom can
be moved
Advantages
No construction
needed
Material is on
site
Disadvantages
Can't control the area
which contains the spi 1
1. Hard to construct
2. Stirred up bottom
1
Divers with pumps
then place concrete
or sand bags around
to form dike if
bottom material
is not sufficient
may cause disper-
sion and Increased
turbidity.
-------
TABLE 19. SPILLS IN WATER - SOLUBLE OR MISCIBLE SPILLS
Method
Sealed Booms
Diversion of
Uncontaminated
Flow
Diversion of
Contaminated
Flow
Gel 1 ing Agent
(40)
Containment
of Enti re
Waterbody
•Applicatlon or
Construction Materials
Boom
Device to anchor
Earthmoving Equipment
Block entrance with
sandbags, sealed
booms or dikes
Gels, Dispersion
Devi ces; use ex-
perienced personnel
Diking Materials
Earthmoving Equipment
Sandbags, etc.
Lining
Use
Contain depth
limited volumes
leaking containers
Advantages
Contain entire depth
of water
Special area where 1. Can put cleaned
topography Is right water Into di-
verted stream
2. Used for flowing
water
Special area where 1. Can put clean water
topography is right back into stream
2. Used for flowing
water
If smal1 volumes
For enti rely con-
taminated area
1. Stop flowing con-
taminant
2. Stop permeation
1. Can allow contain-
ment of a large
waterbody
2. Materials on site
3. Easily constructed
Disadvantages
1. Deployment difficult
2. Not used for large
bodies
3. Difficult to get good
seal (16)
1. Difficult to move large
amounts of earth
2. Clear area needed
3. Impermeability of ground
1. Difficult to move large
amounts of earth
2. Clear area needed
3. Impermeability of ground
k. Adverse environmental
impact
1. Hard to obtain
2. Can't use In large area
3. Must haul to dispose
1. Not all waterbodles have
containable overflow
2. Permeability
3. May be an unstable condition
-------
TABLE 20. SPILLS IN WATER - FLOATING SPILLS
Method
Booms
Wei rs
Pneu-
matic
Barriers
Spill
Herding
Methods
Appl Ication or
construction
materials
Varies; need
deployment
device
Weir £ boat
Air compressor
dl ffuser
deployment
method
Chemicals on
water spray
or prop.
wash
Use
Not too
much current
Calm
Only shallow
water
To protect
shore or
other
facilities
Reference*
p, 6-10 to
6-25
CG-446-4 (41)
p. 6-25
p. 6-25 to
6-25
p. 6-31 to
6-35
Advantages
Used on large area;
Many varieties
Not easily clogged;
Collects S contains
Do not create a
physical barrier
to vessels
Useful in rough
wa te r
1.
2.
Not
I.
2.
3.
I.
2.
Dl sadvantages
Only in waves less
2-k feet
Current speed less
than 0.7 knots
used in rough water
Not in rough water
Only shallow water
Only thin layers
or materials
Not easi ly obtain-
able
Not I00£ effective
Many references are applicable; see Table 16.
-------
TABLE 21. SPILLS IN AIR
Technique
Mist Knock
down
Fans or
blowers
Method
Spray fine mist
into air
Disperse air by
directing blower
toward It
Use
Water soluble or
low lying vapors
Very calm and
sheltered areas
Advantages
Removes hazard
from air
Can direct air
away from
populated areas
Disadvantages
Create water pollution
problem and must be
contained in solution
1. Not at al1 effective
if any wind
2. Need large capacity
of blowers
3. Hard to control
-------
I. Will any natural phenomenon such as rainfall, soil or subsoil
render the containment ineffective?
2. Will man-made conditions such as wells or underground drain tile
render the method of containment ineffective?
3. Is there a sufficient quantity of containment material, personnel
and equipment?
4. Can the containment method be deployed safely and effectively?
5. Can the spill be contained quickly enough by the proposed
containment method?
6. At what point is the containment equipment likely to leak and how
can the leaks be minimized or prevented?
7. Would another containment method be better?
8. Would the repercussion of containment be more harmful than ths
natural dispersal and/or breakdown of the spill?
Figure 31. Establishing the feasibility of
spl11 containment on land
Are there any natural phenomenon such as bottom composition, current,
wave action, access or water depth that would render the containment
method ineffective?
Would man-made conditions such as shipping, concrete channels, or
discharge of dams render the containment method ineffective?
3. Can a sufficient amount of containment materials, equipment, and
personnel be deployed to the site safely?
4. Can the spill be contained quickly enough?
5. Will the spill leak or seep out of the proposed containment device?
If so, can it be prevented from doing so?
6. Would another containment method be getter suited to the spill?
7. Would the repercussions of containment be greater than those of
natural dispersion and/or breakdown?
Hnure 32. Establishing the feasibility of containment
for heavier than water spills
114
-------
1. Are there any natural phenomenon such as discharge volume, spill
! volume, soil structure, bottom composition or rainfall that would
i render this containment method ineffective?
|
i 2. Will any man-made conditions such as dams, concrete channels,
or bypasses render the containment methods ineffective?
! 3. Can a sufficient quantity of containment material, equipment,
j and personnel be obtained and deployed safely?
i k. Can the spill be contained quickly enough by the proposed
i containment method?
I 5. Will leakage and seepage be a problem? If so, how can it be
i ameliorated or prevented?
6. Would any other containment method be better?
I
7. Would the repercussion of containment be greater than those of
natural dispersion and/or breakdown?
Figure 33. Establishing the feasibility of containment
for soluble spi1 Is
1. Will natural phenomenon such as wind, waves, current or tidal
action render the containment device ineffective?
2. Is there any man-made condition, such as, periodic discharge
from dams, water intakes, or boat traffic that would render the
containment device ineffective?
3. Can a sufficient quantity of the containment device be obtained?
A. Can the containment device be deployed safely and effectively?
5- Can the spill be contained quickly enough by the proposed
method?
6. At what point is the containment equipment likely to leak and
how can the leaks be minimized or prevented?
7. Would another containment method be better?
8. Would the repercussion of containment be more harmful than the
natural dispersal and/or breakdown of the spi11?
Figure 3^. Establishing the feasibility of containment
for lighter than water spills
115
-------
1. Will natural phenomenon such as wind or air current disperse
the containment before containment is possible?
2. Can a suitable water collection setup be established?
3. Can the spill be approached safely?
k. Is the material removable by reaction with a water mist?
5- Would the repercussions of containment, especially in creating
a water pollution problem, be more harmful than natural
dispersal, taking adequate safety precautions?
Figure 35. Establishing the feasibility
of air spill suppression
116
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*».*» DECISION ON SPILL HANDLING
k. A. I General
The critical decision regarding handling of the spill is very difficult.
Many variables affect the decision, and these variables must be con-
sidered by the user and altered to fit the specific situation. Only then
can the final conclusion be reached. There are four ways the spill can be
handled: (I) diluted and dispersed into the natural environment, (2)
treated "in-situ" with makeshift processes, (3) hauled to another site
for disposal or treatment, and (k) treated in an on-site, but offstream,
treatment system. The following items are presented to guide the thought
processes of the OSC and allow him to decide on the best course of action
for his situation.
A. k.2 Use of the Thought Guide
The thought guide (Figure 36) is a graphical presentation of the thought
processes required of the OSC when establishing the handling of a spill.
The boxed questions presented are merely summaries of many considerations
which are to be answered by the OSC in establishing the final answer to
the main boxed question. Once an answer of yes or no has been established,
the arrows are followed to the box with the next applicable question. It
is assumed that the OSC is familiar with the manual and can refer to the
following sections which elaborate on the questions, if necessary. The
result of the following thought guide will be determination of a feasible
handling method for the specific spill situation.
*t . *i . 3 Variables to Cons i de r
Determining which of the four methods of spill handling should be used in
a spill situation involves consideration of a series of questions which
affect the choice of handling methodology. The following questions are
outlined in Figure 36. This guide is flexible and is intended to aid the
OSC but not to make the decisions for him. The following paragraphs
outline the considerations which are necessary when the questions are to
be answered.
1. Is the spill contained or containable? - This information can be
obtained by reference to subsection k.2. The size and type of area
affected, mobility of the spill and availability of containment methods
are prime factors In this decision.
2. Is a remote treatment or disposal site available? - The answer is depen-
dent on a wide variety of factors and a series of subquestlons can be
asked.
a. Can the remote disposal site or treatment plant handle this material?
b. Is the volume of the area affected by the hazardous material compat-
ible with the capacity of the remote site?
117
-------
CO
Figure 3&. Spill handling thought guide.
-------
c. Can permission be obtained to use the site for treatment or
disposal of the hazardous material and the affected media?
3. Are suitable vehicles available to haul the affected material?
The type of vehicle required is established by the chemical and
physical characteristics of both the hazardous material and the
affected media. Included in the considerations should be the
fol lowing:
a. State of the material - liquid or solid or percent of each.
b. Corrosi veness of the material.
c. Proximity of sewer lines to allow disposal to a nearby treatment
plant.
d. Other handling properties of the material at the given concen-
tration.
k. Can the spill be hauled within a reasonable time limit?
This consideration includes the establishment of a reasonable time
limit. This limit can be established by comparison to the length
of time to set up and operate a treatment system for on-site
treatment or by other means. If hauling is more time consuming, other
handling methods should be considered. To establish the time for
hauling, the following questions must be answered:
a. Is an unstable weather or physical condition establishing a time
limit?
b. How far away is the remote site?
c. What is the volume of the material affected?
d. What is the truck capacity?
e. How many vehicles are available to haul materials each day?
f. How many and what capacity pumps are available?
The answers to these questions will allow the calculations regarding
the total time required for hauling.
ple of determining if a spill can be hauled in a reasonable time;
Answers to questions - ka~f:
a. I week (before a large rainstorm is expected).
119
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b. l6l km (100 miles) (the distance to a remote treatment plant).
c- 3.78 x 105 liters (100,000 gal.) - volume of affected waterway
d. 8325 liters (2200 gal.) - available volume of septic tank truck
e. 5 trucks are available (number of trucks).
f. pump on truck 373 liter/min (100 gpm) .
Time to fill and empty the truck.
Time = 8325 I (2200 gal.) = 22 min
378 T/m (100 gpmj
Total = 22 + 22 = kh min.
Travel time = 1 6 1 km
ffoTiTTrn (50 mph) = 2 hr (120 min) (one way)
hr
Total = 120 + 120 = 240 min.
Total time + break (10% extra)
23/j + 29 = 3I*» min/trip = 5.3 hr/trip.
Total number of trips required for all trucks
3.78 x 105 I (I05 gal)
8325 I /truck =
How many hours to haul entire amount with 5 trucks?
^tLi£S/J_truck =
5 trucks K
9.2 trips x 5-3 hours/trip = 29 hours
Therefore, I week has 168 hours and hauling can be accomplished within
this time period with a large safety factor.
5. Is hauling politically, economically and technically feasible?
This question combines many of the non-specific variables which must
be evaluated by the OSC. Political opinions may affect the decision
regarding hauling by insistence on a specific and/or immediate course
of action. This position may force the OSC to concur without further
evaluation. Another aspect of hauling is the cost potential. The
economics of both treatment and hauling must be evaluated with the
following considerations in mind:
120
-------
a. Concentration of the contaminant - The more concentrated the con-
taminant, the more likely that hauling will be the most effective
method since treatment by-products may be as voluminous as the
material treated.
b. Amount of solids produced - The amount of solids or sludges
produced by treatment must be considered when evaluating the al-
ternati ves.
c. Amount of treatment by-products produced - The amount of spent by-
products, such as carbon, produced must be considered prior to
haul ing.
d. Solids concentration of the wastewater - The total solids concen-
tration of the wastewater may dictate that the entire volume be
hauled, since these solids will already require disposal.
e. Expense of materials required for treatment - The cost of the
materials required for treatment must be added to the cost of re-
moving any treatment by-products or sludge produced.
f. Specific gravity and solubility of the materials spilled - The
specific gravity will indicate if dredging or skimming operations
can be used to remove the material and the solubility will indicate
the concentration of the materials in a water body. In general,
mostly insoluble floating or sunken materials can be hauled be-
cause of their high concentration, while soluble materials will
usually require on-site treatment.
g. Location of material spilled - Generally, both land and air spills
cannot be easily treated on-site due to the nature of the con-
tamination. Once an air spill has been contained, hauling it to
a manufacturer or other suitable location is generally the most
practical arrangement. Land spills v/i 11 contain high concen-
trations of both the contaminant and other solids, so hauling of
the affected earth can be the most practical approach. Any rinse
water which is used can then be captured and the hauling feasi-
bility for it evaluated separately.
h. Size of the water body affected - Water spills must be evaluated
separately since the effect on the amount of water affected and
the effective concentration of the contaminant must be considered
jointly. Basically, the volume and concentration establish the
applicability of various treatment steps, and the hauling eco-
nomics. Large concentrated spills are most difficult to handle
because large hauling volumes will be generated both with and
without treatment.
The technical aspects of hauling must also be considered. If the hauling
is transposing the problem to a place where more effective treatment or
control is possible, then hauling is feasible. However, if hauling merely
121
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transposes the problem without technical benefits, this approach may not
be the best solution.
6. Are methods available for field treatment?
This consideration is crucial when establishing the viability of
treatment as an alternative handling method. There are treatment schemes
presented in this document which establish methods for treating over
300 hazardous materials. OHMTADS, CHRIS, and other sources may include
other treatment methods and should be consulted. If a treatment method
cannot be found for a certain spilled material, the manufacturer can
be contacted. If still no field applicable method is available,
treatment on the scene is not an acceptable handling method.
7. Is the site available and/or accessible for treatment?
There are certain size requirements that must be met when establfshlna
a treatment site since an offstream plant requires at least 0.20 ha
(0.25-0.5 acres) of area. In-situ treatment requires less area but
accessibility to the spill location is Important to allow delivery of
necessary materials.
8. Can the spill be treated within a reasonable time limit?
Treatment feasibility is also contingent upon the amount of time
necessary to treat the wastewater. This time limit may be established
by unstable weather conditions that would cause the spill to spread or
by economic restraints caused by manpower costs. The following cate-
gories should be considered:
a. Length of time to construct treatment process.
b. Total flow through rate of operation.
c. Total amount of material to be treated.
d. Number of hours of operation per day.
Example: a. 43 hours (to set up equipment).
b. 189 l/min (50 gpm) (flow rate through plant).
c. 3-78 x I06 I (I06 gal.) (amount of water to treat)
d. 16 hours/day (hours of daily operation)
Total time = [48 hrs + (3-78 x IP6 I ) ] I
(189 l/min x 60 rnjjn,) T6 hr/day ~ 2k 'days
hr
122
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9. Are supplies available for safe treatment?
Included in the considerations for this question are: The volume and
cost of supplies; the length of time for delivery; and the materials
necessary for safe handling of chemicals. If any of these considera-
tions indicate proper materials are not available, the answer to the
main question is considered negative.
10. Is in-situ treatment applicable?
At first inspection, in-situ treatment would seem to be the best
method of treatment for the following reasons:
a. Handling of the hazardous material is minimized.
b. Construction time and land requirements are substantially reduced
or eliminated.
c. Treatment can be done on the entire system at once.
In certain situations such as where efficient treatment is not necessary
when the time to treat is not critical, when the water volume is
extremely great or when no significant amounts of byproducts are
produced, in-situ treatment becomes more advantageous. However, it is
necessary to evaluate the end products of the process and consider
other aspects on in-situ treatment before it is implemented. Im-
portant considerations include:
a. Can in-situ treatment methods achieve the degree of treatment
requi red?
b. Are significant amounts of sludge produced which may either harm
the benthic population or require additional removal?
c. Can in-situ treatment accomplish the task in a reasonable amount of
time or would an offstream process be faster?
d. Are dangerous by-products formed or is there a general change in
the water chemistry which is harmful to existing fauna and flora?
e. Is the method safe for personnel employing it?
Once these factors have been considered, the choice of treatment type
can be made.
II. Is remote hauling still impossible?
This question provides for re-evaluation of the hualinq question. At
this point, it is assumed that on-site treatment either in-situ or
offstream is not possible due to negative answer to any one of
123
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Questions 6-10. Therefore, the feasibility of hauling as indicated
by Question 5 must be re-evaluated. It is best to reconsider all the
questions (2-5) to determine the hauling feasibility. If this question
still results in a negative answer, dilution and dispersal is the only
alternative left.
12. Are safe methods available for "in-situ" treatment?
This question initially assumes that the spill is not contained or
containable. Then the methods for in-situ treatment must be con-
sidered. Both flow-through and "batch" methods and the effects of
these procedures and their by-products must be established. Among the
pertinent questions are:
a. Is a reasonable in-situ method available? When in-situ treatment
is not possible, dilution and dispersion is the only available
handling technique.
b. Is the treatment effective to achieve desirable removals?
c. Are by-products produced which are harmful to the aquatic en-
vi ronment?
d. Can the materials be assembled in time for in-situ treatment?
Ttiis is a critical immediate concern for an uncontained spill. Both
the specific chemicals or chemical products and the construction
material must be obtained in a short time to determine if in-situ
treatment is feasible. Where this is not possible, dilution and
dispersal must be used.
4.5 HANDLING A SPILL BY HAULING
Once the decision has been made to haul a spill the following specific in-
formation must be gathered by the OSC:
I. Determine the hazard potential and corrosivity - the specific problems
in handling are outlined in many handbooks and any special equipment
must be obtained.
2. Calculate the total volume of material to be handled.
3- Obtain suitable hauling vehicles:
Liquid spill: septic tank truck
tank truck
rai1 road tank car
empty barge
cargo ship
-------
Solid spill: sealed dumpster (small volume)
lined and covered dump truck
lined and covered railroad cars
b. Obtain pumping or transfer equipment and estimate the rate of transfer
of material.
5. Estimate the total time to haul the entire spill:
The calculations are summarized as follows:
Total spill volume ., , , . . . ,
r,—i—• •• •'v—.• ,— = Number or truck loads
Volume or 1 truck
Number of truck loads Number of loads
s ____^___*_****_
Number of trucks 1 truck
Volume of 1 truck _ = Number of loads
Loading Rate (pump etc.) 1 truck
Travel distance 0 T , T.
,,-.• , -;— x 2 = Travel Time
Highway speed
I.I (Travel time 6 fill and draw time) = Total Time/Load
Total time/load x Number of loads/truck « Total time/truck
Total time + Fill time x Number of trucks = Total time to haul
truck (assuming staggered fills)
I*.6 HANDLING BY DILUTION AND DISPERSAL
Only after all other possible alternatives have been investigated and found
not to be feasible is the method of handling by dilution and dispersal to
be considered. This method must be used only as a last resort to minimize
local hazards. Care must be taken to determine if this method is feasible
in that mixing the hazardous chemical with water does not cause undesirable
side reactions or by-products. Once it has been determined that dilution
and dispersal is the only action available, then additional water sources
must be brought to the spill site. Water should be added to the stream at
a turbulent spot to allow complete mixing with the hazardous material.
Care should be taken not to exceed the capacity of the water body and
extend the hazard past its natural boundary. Dispersion can also be in-
duced by creating mixing zones in the waterway and reducing the pockets of
concentrated contaminant which may exist.
k,7 HANDLING BY TREATMENT ON SITE
125
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/t.7- I General
Once it has been established that treatment of the spill on-site is the
nost feasible approach, then the method of treatment must be chosen. At
the present time most in-situ treatment methods are experimental and there-
fore, have not been included as prrt of this review of state-of-the-art
processes. The emphasis instead has been placed on construction of
offstream processes and therefore leads directly into Chapter 5.
Unit processes have been chosen that have features applicable to jury-
rigged construction. The possible processes were evaluated according to
the following criteria:
I. They should be capable of being set up in one to two days, and there-
fore, must be constructed of readily available materials, and should
be of simplified construction.
2. They should not require large amounts of power or other supplies.
3. They should be flexible and capable of operating under a wide
variety of conditions.
Many types of wastewater treatment systems were considered and 5 were
chosen: filtration, carbon adsorption, ion exchange, gravity separation
and chemical reaction (oxidation/reduction, neutralization and precipi-
tation) .
The processes will be integrated into a parallel batch system which allows
the flexibility and simplified operation of a batch process and yet al-
most continuous operation
4.7.2 Specific Treatment Schemes
Treatment schemes have been suggested for the 303 chemicals indicated on
EPA's modified list of hazardous chemicals (|8)« It must be emphasized
that the schemes have not been field tested and extreme care must be taken
in their application. The information regarding the schemes indicated
in this chapter was developed from several different references, common
industrial waste treatment schemes and the experience of personnel
familiar with chemical wastewater treatment. The schemes are intended to
direct the people but may not be applicable in all situations. The
following considerations were used in developing the treatment schemes:
!. The chemicals are assumed to be relatively pure and free of major
chemical interferences during treatment.
2. All schemes are established to handle chemicals in an aqueous system
and in water.
3- The dosages of treatment chemicals needed will be established by on-site
126
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testing of a sample of contaminated water. These field tests will
also aid in establishing problems which may occur during field treat-
ment .
k. Gravity separation was included as a requirement or an option in all
shcemes. This separation process should always be considered since it
will reduce the chemical demand of the waste and allows a natural con-
centration of contaminants.
5. Filtratio"! is included as an additional clarification step to allow
carbon adsorption and ion exchange processes to operate more
effi c iently.
G. Filtration is also used to remove the fine suspended materials after
certain precipitation reactions which require highly efficient re-
movals (19,2C).
7- Additional pretreatment requirements such as a presettler or filtration
must be evaluated by the user.
3. The schemes indicate batch processes in series, however, sometimes
more than one process can be done in the same tank. This is usually
true when no sludge is produced in the reaction. However, if a sludge
is produced, series tanks are necessary to avoid negating the effects
of the previous operation.
The final consideration for all treatment schemes is determining if the
treatment is complete and discharge is acceptable. The effluent quality
achieved by a certain schematic is dependent upon many variables in-
cluding strength of the waste, chemical interferences in the water body,
etc., and cannot be predicted before a spill event. The discharge con-
centration level must be established depending upon the individual spill
situation and the effluent must be tested prior to its release into the
surrounding waters. Depending on the complexity of the analytical method
required and the proximity of capable laboratories, it may be necessary
to hold the effluent from the process for a certain time period. There-
fore, extra tanks must be supplied to provide the necessary detention.
These tanks must have a capacity which will equal the amount of flow that can
be treated during the duration of analytical test, plus the amount treated
during the time it takes to empty one of the tanks, plus the amount
treated during the time it takes to fill one of the tanks. Obviously, a
higher number of smaller volume tanks will result in less total tank volume
required. The number of tanks can be calculated as follows:
- Volume treated during analytical period + 2
Number of tanks = rr~, r~—;—;—: T
Volume of tank being used
The treatment schemes as shown in Table 22, convey specific information
about the treatability of the 303 hazardous compounds. Each column in the
table conveys specific information which is discussed below:
Column I - Name of Compound One of the 303 hazardous materials.
127
-------
Column 2 - Amenability to Treatment
in a Municipal Treatment
Plant -
Column 3 - Treatment Scheme -
This indicates whether the
material can be discharged to
a municipal treatment plant
without creating major up-
set. The specific plant
operator must be consulted
before a final decision can
be made.
This column indicates the
applicable treatment scheme
and options for each che-
mical. The symbols used
are defined as follows:
o-
I A
F
Batch Process
- Flow Through Process
- Optional Process
- Recommended Process
- Carbon Adsorption
- Dual Media Filtration
- Ion Exchange
- General Chemical Reaction
- Reduction
- Oxidation
- Gravity Separation
- Precipitation
- tleutral ization
- Di1ut ion
The treatment chemicals are Indicated by arrows Into the specific unit pro-
cesses and as Indicated previously, more than one process nay be done in one
tank.
Column *4 - Treatment Specifications
The endpolnts for determining
chemical dosages a'-*e briefly
indicated.
128
-------
Column 5 ~ Comments
Column 6 - References
Column 7 ~ Provisional Limit
This gives additional infoi—
mation which may be helpful
to the user. This may in-
clude specific hazards or
methods to simplify treat-
ment .
The reference column is
intended to allow the user
to have more information
regarding treatment schemes
or the bases of the schemes
as presented. It must be
recalled that the processes
have not been field tested
and care must be taken in
their application. In some
cases an asterisk (») has
been included which in-
dicates that the process as
described are theoretically
possible but no reference
was available which could
verify the technique.
Additional care must there-
fore be taken when per-
forming bench scale tests
and effluent analyses are
crit ical.
The provisional limit de-
fines acceptable levels of
exposure of the working and
general population and eco-
logy (15). The levels are
very conservative so the
OSC must remember to take
into account dilution by
the natural water body
which may allow the effluent
level to be many times
higher than that listed.
This limit is intended as a
guideline, however, the best
procedure is for the user to
establish the acceptable
discharge level for the
specific material by consult-
ing local authorities. This
129
-------
number is not indicative of
the effluent quality
established by the treat-
ment scheme.
Once the chemical has been located on the table, the user can then use the
information to determine the amount of chemicals or materials needed for
treatment. The treatment specifications and bench tests will allow the user
to calculate the amount of chemicals to order.
The carbon amounts are indicated in weight of carbon per weight of soluble
material. Therefore, to calculate the total amount of carbon, the solubili-
ty of the spilled chemical and the volume of water affected must be known.
The carbon amounts ordered should be based on the highest number in the
range presented. Then as the carbon is spent during treatment, the volumes
should be checked to determine if more carbon is needed. The numbers given
were divided into various ranges depending on many factors including ad-
sorbability, toxicity and solubility. The following assumptions were made
in establishing the values presented:
I. To reach low levels, much more carbon is needed even for strongly adsorbed
materials.
2. All insoluble material will be removed by sedimentation and filtration
prior to the carbon column.
3. Carbon demand by other organics is not great.
k. Compounds with low solubility and high toxicity will be treated to low
contaminant levels and require high carbon doses.
5. Less toxic materials will not require low efficient concentrations so
less carbon is needed.
It is very difficult to attain both effective cont-ict time and control of
carbon columns in the field, so a series operation is recommended. Samples
can then be taken between the two columns to predict when breakthrough will
occur. The columns should also be operated countercurrently to allow most
effective removal of the contaminant.
To use Table 22 effectively, the following procedures should be followed:
I. Turn to the specific chemical name which is to be treated.
2. Establish the possible treatability through disposal to a sewage treat-
ment plant.
3. If disposal to the sewer is not feasible, go on to determine the appropri-
ate treatment scheme.
130
-------
k. Note the treatment specifications and cotnients which apply to the spill
si tuation.
5. Go to specific references to collect additional information if necessary.
6. Turn to individual sections on process descriptions and perform out-
lined bench scale tests.
7- Calculate and order amount of chemicals and other material needed as
outlined.
8. Start process construction by reference to the system design, Chapter 5 6 6.
A.7• 3 Treatment of Hix_tu_res_
The treatment schemes as presented in Table 22 deal with individual hazard-
ous chemicals and to not specifically consider the numerous problems
associated with treatment of mixtures. If a spill of mixed chemicals has
occurred,extra care must be taken during all steps of identification,
assessment,and treatment. The following procedures should be followed:
I. If the identity of one or more of the chemicals spilled is not known,
do not approach the spill site.
2. If the identity of the chemicals is known, determine the compatibility of
the spilled compounds. To do this, make preliminary reference to the
compatibility chart included in Table 10. Then contact the chemical's
manufacturer or local University Chemistry department for more infor-
mation.
3. Establish the identity and amount of reaction products from the above
sources or reference to chemical handbooks.
A. Choose a possible treatment scheme to remove the reaction product_or rz-
actant. Removal of the product or reactant should force the equilibrium
of the reaction in the desired direction. However, the treatment scheme
chosen should be verified with the consulting chemical authority.
131
-------
TABLE 22. SUGGESTED TREATMENT SCHEMES
v-o
N3
Amenable Prov.
Biological Trmt . Treatment Limit
Chemical at Municipal STP Treatment Scheme Specifications Comments Reference mq/l
Acctaldchyde When diluted Backwash
H n
9 r.?c-inn am <;^i nilnto if 'n H, q.O
J- |J-, p-U 1 Matl. necessary/ 21,22
1 5 1 *|^| •[ A | — *—•• compound may
t volat i 1 i ze
sol ids
Backwash NaOH
and diluted i 1 J-. JL send to STP if 21,22
'S) — "j F | — H A r^ty— *- 2 . Neutral i ze with poss ib le/other-
NaOH to pH 7/send wise treat wi.th
. to STP. carbon/ ion ex-
I*S^ m(n\ STP change may also
" •-' \ — ' be used
Acetic When neutralized Reacts with water
Anhydride and diluted See Acetic Acid to form Acetic '0,1^ '-°
acid
Backwash HCI
Acetone May require j li \
Cyanohydrin acclimatization ( Sy — ^CR) — *l ^ r
Sol ids
Backwash
Acetyl When diluted , -*^ r-j-| j-^-)
Bromide \?J T—J TlLr
sol ids
Acetyl When diluted See Acetic A
Chlor ide
— T^|— "VVT*" Neutralize with Raise pH to 10,15 2-°
1 NaOH to pH 8.5 suppress cyanide
H2° Adsorb/neutralize gas formation but
to pH 7. not greater than
C- 10- 100 H/H Sol. pH 9
NaOH Matl.
./ik . After Adsorption Dred9e PumP or U,1S °-°5
^ add NaOH to pH vacuum undissolved
7 from bottom.
C= 10-100 It/11 Sol. Decomposes to
Matl form Br and HBr
cid Reacts with water to 19 0.05
form acetic acid
and HC1
-------
TABLE 22. (continued)
Hazardous
Chemical
Amenable to
Biological Trmt.
at Municipal STP
Treatment Scheme
Backwash NaOH
Treatment
Spec i f icat ions
r • in. inn #/# c_i
Prov.
Limit
Comments Reference mg/1
Acrolein
When neutralized
dilute/acclimated
system desirable
Matl. then NaOH
or other base to
pH 7.
route to STP if
possible (use
air) - extremely
poisonous and
explosi ve
10, 19
0.01
HC1
H20
Acrylonltrile When diluted/ |. (.
may need to be "i
acclimated solids
NaOH
then HOC1
2. (§)—®—
To STP
Adipontrile When diluted and
acclimated
See Aerylonitri 1 e
Add NaOH to pH
8.5/adsorb/
neutralize to
pH 7 with HC1
C: 10-100 #///
sol. mat) .
Add NaOH to pH
10 then add
HOC! to a
residual react
30 min./ dis-
charge to STP
Uquid is flam-
mable and
explosive - Care-
ful to avoid HCN
evolution or
direct contact
with NaOH. Option
2 produces
cyanates which
are less toxic
10. 19
2.0
1.25
-------
TABLE 22. (continued)
Amenable
Biolog ical Trmt .
Chemical at Municipal STP Treatment Scheme
Backwash
-L?,-^]-[i}-.
sol i ds
Backwash H n
Al lyl When di luted 1 1 I ?
A'coh°' ^S) n|~M -FA"! i«-
f
Solids
Ca(OH)2 or I^COj
Ally! When diluted j[ i 1 1 Backwash
Chloride and acclimated (S ^K^)~n^r~>fM — "
-^ v-x
Ca(OH)2
Aluminum ._ JL , .
Sulfate When diluted ~*CO — "vD — "LLi"*"
T
HCI
nu i
Ammonia (in When diluted 1 . — K^)-— STP NaOH
water aqueous (and neutralized "21 *t i
ammonia or if necessary) f ^j-^/rRV-JTT— JTJ3WNV-— »
ammonium ' pT^ — ^ —
hvdroxide) 41 1
Backwash
Sol ids
Treatment
Specif icat ions
C: 100-300 #/#
sol . mat 1 .
C: 35-100 It/If
sol . mat 1 .
Add Ca(OH)2 to
pH 6-7 / adsorb
and discharge
C: 10-100 A/#
sol . mat 1 .
Add Ca(OH)2 to
pH 6-7/f i 'ter
and discharge
\ . Neutral ize to
pH 7 with HCI
2. Add H SO^ to pH
6-7/exchanae/
neutral ize to
PH 7
Prov.
Limi t
Comments Reference mg/1
Vacuum dredge 10, 19 0.012
or pump un-
dissolved por-
tion from bottom
(if wettable
powder) skim if
wettabl e oi 1
Discharge to treat- 10, IS 0.23
ment plant if
feasible; may require
d i lut ion after
adsorpt ion
H i gn 1 y f 1 ammab 1 e ; 1 0 , 19 , 0.15
hydrolyzes to allyl 23
alcohol in aqueous
solution; however,
since slow to dissolve,
use boom or sorbants
if si ick exists
Hydrolyzes in water 10, 19, 250
to reproduce aluminum 2k (as SO.)
hydroxide (white)
precipitate/add poly-
electrolyte if needed
for settl ing
Ammonium will exert 10, !;»,
oxygen demand on re- 25 0.01
celvlnci body unless removed
or oxidized. Adjusting
pH to 6 insures forma-
tion of NH.+ if needed
for res i n .
-------
TABLE 22. (continued)
UJ
Amenable to
Hazardous Biological Trmt.
Prov .
Limit
Chemical at Municipal STP Treatment Scheme Specifications Comments Reference mg/l
Ammonium ., . . , . Dilute discharqe to 10,19,25
. if neutralized See Ammonia , .?
Acetate reach acceptable
acetate levels
Ammonium ., .. , . Dilute discharqe to 10,19,25
„ if neutralized See Ammo n a , .,
Benzoate reach acceptable
benzoate levels
Ammonium ., ,., r „ • 10,19,25
„. , if neutralized See Ammonia
Bicarbonate
Backwash
Ammonium if neutralized
Bisulfite & oxidized 1
(s)-^oWN>
V-/YY
HOC! HC1
Add HOC1 to a residual/ Oxidation can 10.19,25
1 1 react 10 mi n/neut ral i ze occur before
-J F 1 — •lixl 1 to pH 7 w HC1 /filter/ ammonium removal/
1 place throuqh ion if STP available,
— - exchanqe media/add discharqe there
QO*— ' MaOH to pH 7 if needed
M ~nu
„ . if neutralized See Ammonia Dilute discharqe 10,19,25
Brom ide , .
to reach acceptable
bromide level
Amn---ium . , .. , Dilute to reach 10,15,25
. , if neutralized See Ammonia
Carbanate acceotable carbo-
nate level if
necessary
. , if neutralized See Ammonia Dilute to reach 10.19,25
Carbonate ._ . .
acceptable carbonate
1 evel s
Ammonium i f neut ra 1 i zed Se(. Ammonia D i 1 ute to reach 10,19,25
Chlor ide , , . , , . .
chloride discharqe
levels if necessary
0.01
(NH,)
J
0.01
(NHj
0.01
0.01
(NHj)
Q.OI
q.oi
(NHj)
0.01
(NH,)
0.01
(NH3)
250
(cD
-------
TABLE 22. (continued)
cr.
Amenable to
Hazardous Biological Trmt.
Chemical at Municipal STP Treatment Scheme Specifications Comments
Ammon ium. . , . . „
.... if neutralized See Ammonia
c i trate-
D i 1 ute if
necessary
Reference
Prov .
Limit
mg/1
Ammonium unknown No treatment scheme
Fluoroborate recommended
Ammon ium . - . .
... . . it neutralized See Ammonia
Hydrox i de
Ammonium if neutralized i HI 1
Hypophosphine £• oxidized (; 1 WN) ^Trl
\_'~^;i/ L_Lr
N !• 1 D V«
1^ I ry*
HC1 Ca(OH)
"
at this t ime
•'•
10,19,25
| Add HC1 to pH 7/filter Removal of pho- &0.19.25
.r!~| £ exchange in weakly sphate should
' — 1 acidic media/oxidize occur after ex-
0.01
0.01
as NH
to HOC 1 residual/add change to avoid
f^\j, Ca(OH)., and some CaCl^ ren«Dv!nq excess
^^f to pH 1 I/neutral ize cations from
sol-
* . to pH 7 ution/CaCU will
2 HUU allow sludge vol-
ume to be reduced
CaC12 by adding Ca(OH),
if more ppt/con-
Ammon i um
Iodide if neutralized See Ammonia
t inue unt i 1
ppt forms
no
Dilute or reach 10,19.25
acceptable Iodide
Ammon i um
Nitrate neutralized See Ammonia
Oxalate if "«"tralized Ca(OH)
1 i Hi'
(syVpV-^iv-4n-
concentration
Dilute or remove 10.19.25
with anionic
exchange resin
Ca(OH) Add Ca(°H'2 to pH ?/ Oxalate should
1 f 2 ppt oxalate/neutral ize removed in the
JJY|_«^ly-. w HCI to pH 7/filter precipitation
be 10,19,25
1 ime
steo
0.01
as Nh,
3
0.01
as NH,
3
as NH,
3
exchange/neutral ize
with base to oH 7
-------
TABLE 22. (continued)
Hazardous
Chemical
Ammon i urn
Pentaborate
Ammon i urn
Persulfate
Amenable to
Biological Trmt.
at Municipal STP Treatment Scheme Specifications Corrments Reference
When neutralized See Ammonia
and di lute
When neutral -Na|is"'f'%OH
Ized and (TWjX^VjtV
dilute \3/^>^vyn — r
Dilute to reach ac- 10,19,25
ceptable Pentaborate
i i eve i s .
NaOH
I 1 Add H SO, to pH J,/ Special indicator is 26
J^X~L»/N)— » add bisulfite to large Methylene Blue in 50%
'—— * ^—^ ORP change or indica- solution of Zinc Ace-
tor change/neutralize tate - add 0.5ml to
to pH 7/fi'ter exchange 1 drop of test solu-
neutralize to pH 7 with tion/stays violet
NaOH often. until persulfate is
gone - *hen color is
not violet reaction
is done - test often.
Prov .
L i ,T i t
mg/ i
0.01
fls NH _
0.01
as NH-
Ammon i urn
Si 1icofluoride Unknown
Ammon i urn
Tartrate
Ammon i urn
Th iocyanate
Ammon i urn
Thiosu1 fate
When neutralized
and d i1ute
When neutralized
and dilute
When neutralized
and di lute
No treatment scheme
recommended at this
time- Backwash
H.,0
See Ammonia
See Anmonia
Add HC1 to pH II
fi 1 ter/exchange/
carbon can be used
to remove tartrate
Dilute to meet tartrate10''
standards on carbon
If desired, thiocyanateI0>'9»25
can be oxidi2ed further
with HOC1.
Dilute if necessary '0,19,2?
0.01
as NH,
0.01
as NH,
0.0)
as NH,
-------
TABLE 22. (continued)
10
oo
Hazardous
Amenable to
Biological Trmt.
Chem'c--1' et Municipal STP Treatment Scheme Specifications
Ammon i um
Sulfamate
Ammon i um
Sulfate
Ammon i um
Sulfide
Ammon i um
Sulfite
When dilute 1 HOC1 HC1
and neutralized Jk. JL JL JL
( A^~*\°)~*vNy~*1 F
When neutralized See Ammonia
Backwash
II
„.., „„ . H°C1 HCJ
and neutralized *. JL JL j-L-i
(S )-*fO>WN >-MF r*
V — r^O'V_/ I—- I
When oxidized See Ammonium
and neutralized Sulfide
I
Chlorinate w hOCL to
1 [-^ residual/react 5 min./
r*yX| — 1 neutralize to pH 7 if
1 needed/filter/exchange
^~ 1 in weakly acidic resin
QO* neutralize to pH 7 with
T NaOH.
NaOH
NaOH
. Add HOCI to residual
r— lA_^react 5 min./neutra-
liiPVEL/^ 1 i ze to pH 7 with HC1/
filter/exchange on
weakly acidic resin/
neutralize to pH 7 with
NaOH.
Comments Reference
Sulfamate must be 10,19.25
rentuKerf prior to
ammunio trmt. since
it converts to NK3
and H-SO^ when oxi-
d ixed .
Dilute if necessary 10,15,25
to meet sulfate
discharge levels
Take care to avoid 10,1^,25
inhalation of H,i-
a self contained
breathing apparatus
is recommended.
10,19,25
Prov.
Limit
nig/1
0.01
as NH
0.01
as NH
250 a
so.
0.75
as H2
0.01
as NH
0.10
as
3
5
s
3
Sulfate
-------
TABLE 22, (continued)
Amenable to
Biological Trmt. TreatmenJ
Chemical at Municipal STP Treatment Scheme Specifications
Backwash
Amy! Acetate When diluted __/k_rL1_rJ-|__ C: 10~100 #/#
*xl/l__J *1 " 1 to sol. matl.
Scum
Backwash
Aniline When diluted with JL J-.
time for seed — *< S )— *j FJ—
acclimation I
(activated sludge) Solids
NaOH s"
Antimony Not unless i i
Pentachloride treated first ("£)_^pVyp\-J~
[ Sb2o3 Ib2s3
NaOH
Antlmrttw Pnt . Hot unlp^i "*" -*
jJ-j C: 1-10 #/# of
*1 A I — •• sol . matl .
Na2C03 air
1 i Add NaOH to pH 7/
n_»/NY*/oy» ppt oxide/then
-1 ^^ ^-^ saturate w/S" to
residual/settle/
f 1 Iter/neutral Ize
w/soda ash -pH 7/
aerate to remove
excess S*
3°H u ^ Add MaOH «r> nH 7/
Comments Reference
Remove floating 10, 19
port ion asap;
soluble to 850 ppm.
Dilution & discharge
may be feasible
Slightly heavier than 10,19,27
water so dredging may
be necessary. Produces
poisonous gas if heated
Chlorine gas may be 1,10
formed from this com- -
pound. Be careful not
to add excess S* and
produce H_S toxic gas
Prov.
Limit
mg/1
26.3
0.95
0.05
(asSb)
n nc.
oot oxide/then
saturate with
Na.S to residual/
seltle/fiIter/neu-
tral ize to pH 7.
Aerate if necessary.
as Sb
-------
TABLE 22. (continued)
jr-
O
I'az^rdous
C emical
Antimony
Tr i bromide
Ant imony
Trichloride
Antimony
Trlf luoride
Antimony
Tr i ox ide
Arsenic Acid
Arsenic
Oisulf ide
Arsenic
Pentaoxide
Afier.eble To
biological Trrnt.
at Municipal STP Tree fnent Scname
no See Antinx>ny
Pentachloride
n° See Antimony
Pentachloride
no See Antimony
Pentachloride
no Same as Antimony
Pentachloride
Backwash H sn
,£) ./"pY T/F) *(n) •-
sol ids & Fed 3
NaOH or HC1 H 0
no _ i. j — . P
( S ) — *\ P) H F 1 — *-"•
solids \
As.S,
no See Arsenic Acid
Treatmen •.
Spe.cif icat ions
Add 1 ime to pH
10.5 then add
Fed 3 to form
floe/settle 6
f i 1 ter/neutra-
lize.
Change pH to 6-7
and allow As_S, to
preclpltate/f i 1 ter
£ dilute if neces-
sary
Comments Reference
Check to insure 10,19,20
acceptable bromide
level in discharge
Check to insure ]g 26
acceptable chloride
level in discharge
Check to insure 19.20
acceptable fluoriuc
level In discharge
13.it
'
Arsenic acid converts 20*
to Arsenate in water
with 02 present/will
be caught with ferric
hydroxide £ removed
Dredging may be required 20t^k
si nee As,S_ is qui te
22 ^
Insoluble. Add Fed,
and alum to aid
clar if icat ion
Dredge undlssolved 20
portion from bottom
Prov.
L i n i c
F'O ' }
0.05
as Sb
0.05
as Sb
0.05
as Sb
0.05
0.05
as As
0.05 as
As
0.05 as
As
if necessary
-------
TABLE 22. (continued)
Amenable To
Hazardous Biological Trmt-
Chemical at Municipal STP Treatment Scheme
Ca
f i 1 ter/ neutral i ze
to pll 7/discharge.
Comments Reference
Evolves HCI in \ v, 20*
water. Soda ash
ur bicarbonate
can be used U>
suppress HCI
evolu t ion
Oreuye purnp or 10,19,20
vacuum precipi-
tate f ;MI.-. bottom
10,15,20
9 0
L. -J
.
The arsenite is 2^
oxidized to
arsenate which
is treated as
before.
20
Prov.
Limit
my/1
0.05
0.05
as As
O.C5
^ 1 Ar
d > MS
0.05
as As
0. 05
as As
0.05
as As
-------
TABLE 22, (continued)
Hazardous
Chemical
Potass i um
Arseni te
Sodi um
Arsenate
Benzene
Amenable To
Biological Trmt.
at Municipal STP
no
no
When di luted
Treatment Scheme
See Calcium Arseni te
See Arsenic Acid
ri,im Backwash
A-rh-rii-
Treatment
Specifications Comments Reference
10.19,20
20
C:IO-35 #/# sol. Skim off surface if 10,29
Prov.
Limit
mg/1
0.05
as As
0.05
as As
3.5
matl .
possible.
NaHCO,
Benzole
Acid
When di luted
H 0
N>
Sol ids
insoluble acid
Backwash
Add NaHCO.to pH Dilute waste w/water
7 after sedimen- to allow discharge
tat ion has removed into water body after
most insolubles. neutralization. Carbon
C:10-35 #/# sol. may be used to remove
matl. contaminant
19
1.25
backwash
Benzon i tri 1
solids
C:35-100 #/# sol. Overnight holding may
matl. Adjust pH be required to Insure
to 8.5 to suppress complete reaction.
HCN formation
28
0.01
As CN
NaHCO,
BenzoyI
Chloride
After
with NaOH
sol ids
Add bicarbonate
to pH 7-8; Adsorb
on carbon.
Send to STP if
possible/if removal
needed adsorb on
carbon. C:10-100
#/# sol matl.
'5,28
0.45
-------
TABLE 22, (continued)
Hazardous
Chemi ca 1
Benzy 1
Chloride
Be ry 1 I i urn
Chloride
Be ry 1 1 i um
Fl uori de
Be ry 1 1 i um
Ni trate
Brucine
Butyl
Acetate
Amenable To
Biological Trmt. Treatment
at Municipal STP Treatment Scheme Specifications
Backwash
Use NaOH to con- 1. 1 [" " ] 1. L: 10-100 tl/ti
vert to alcohol; (s) — J~F~1 J~AJ sol. matl.
then biodeqrad- ^f ' — ' •—— '
able NaOH 2. Neutralize to
2 (^\ *(u\ * to STP pH 7 £ route
• \^> ^y to STP.
x->. /^\ _s~*\^ 3- Cone, solutions
3- (£) \?) "Vy—*" only/add lime or
(concentrated only) soda ash to PH 1
dispose solids
properly neutralize
Backwash u cn any effluent
1 Ca(OH)2| 4 A
no i ,A\ J~> -ATN Add lime to PH 8-5"
(.^~Kj9~^LFJ~~*vy~'" 9 let react 15 min.
] settle (filter if
solids needed) /neutral ize
to pH 7 w/H2SOJ).
Na,CO,/Ca(OH)7
no z i L HCI Add Ca(OH) to pH
^ JL r -, JL H20 8.5-9/settle/decant
^ — K^)"*!.1!! Cl!/~* /add lime to pH I I/
"" let stand 2A hr/f i Iter
if necessary /neut. to
pH 7 with HCI.
no See Beryllium Chloride
Backwash
no /sv— JTT— JA!— +• C: 10"100 W
^' *1 1 i — 1 sol. matl.
f^\ .[~n J~n _ tests should be
Prov.
Limi t
Comments Reference mq/1
Can form HCl-if 19,28 0.25
concentrated haul
to manufacturer if
possi ble.
Be sure to di lute 10,19 1.0
the Cl to an ac- as Be
ceptable discharge
concentration 250
as Cl-
Must remove Be and F 26 1.0
in subsequent pro- as Be
cesses.
Dilute system so 19,26 ],0
nitrate discharge as Be
is acceptable.
30* 1*5
as NO,
Skim off quickly 10,19 35.5
to reduce load on
Skim
SolId<:
done C: 1-10
#/# sol. matl.
carbon column.
-------
TABLE 22, (continued)
Hazardous
Chemi cal
Buty lamine
Amenable To
Biological Trmt
at Municipal STP Treatment Scheme
"Backwash
When diluted j^ ] \
Treatment
Speci f ications
C: 10-35 #/# sol.
mat 1 .
Comments
Send to STP if
possible.
Reference
19.31
Prov.
Limit
mg/l
0.75
Butyric Acid Can be discharged
after neutral Ized
Backwash
C: 10-35 #/# sol.
mat!.
No treatment per se
g!ven ; dilutton to
below toxic level is
necessary if no STP.
28*
Cadmi urn
Acetate
Backwash
Backwash
2. J Ca(QH)
so ids
Add 1ime to pH
10/mix/flocculate
& settle/add HO
to pH 7
C: 10-100 #/# sol.
mat).
Cadmium cannot be
removed if CN~ is
present/prior CN~
removal is required/
iron addition may
increase Cd removal/
di lute acetate i f
necessary.
19.20,2**
0.01
as Cd
Cadmi urn
Bromide
See Cadmium acetate
Dilute bromide to 19,20,24 0.01
acceptable level. as cd
Cadmi urn
Chloride
See Cadmium acetate
The precipitation 19,32 0.01
reaction is recom- as cd
mended for removal
at low concentrations. 250
However, C adsorption as Cl
is also effective/
di lute O" to <250 mg/l
if needed.
-------
TABLE 22, (continued)
-e-
vn
Amenable to
Hazardous Biological Trmt.
Chemical at Municipal STP
Calcium no
Carbide
Treatment Scheme
Backwash
Calc i um
Hydroxide neutralization
Backwash
CaIc i urn
llypochlor i te
Na Bisulf.lte NaHC°3 H0SO,,
CaIc ium
Oxide
when
neutral ized
See Calcium Hydroxide
Captan
Carbary1
(Sev i n)
After reduction
w/calcium hypo-
chlorite for 2*»
hours
Carbaryl
£ Sol ids
Treatment
Spec!ficat ions
Add sodium bicar-
bonate to pH 9;
allow to sett 1e;
neutraIi ze to pH
7; dilute to reduce
C 2^2 con cent rat ion
1. Settle and neut.
HC1 ; dilute ;
d ischarge
2. To remove calcium:
add HC1 to pH 7;
then add Na2CO., to
pH 9; settle; fi1ter;
neut. with y^SOj,
Add acid to pH 3;
then b isulfi te unt i1
no chlorine residual;
after 15 min. add UatlCO,
to ppt calcium carbonate
pH 9; neutra)ize;
d i scharge
Add acid to pH J; then
add Na2COj to pH 9; ppt
CaCOj; neutralize to pH ~]
C: 100-300 f/f
sol. mat 1.
C: 100-300 #/#
sol. ma11.
Carbaryl will be removed
during sedimentation
Comments
Reference
Take car to ovoid 10,19
explos ion from
vapors (C2H2) ;
discharge when
cone . i s accep-
table
Dilute ulti 1 CaCI 10,19
by prod . cone . i s
at acceptable levels;
Use 2. i f Ca must be
removed
Other reducing
agents: sod i urn
tniosulfate,
ferrous salt, etc.
can be used
Poss i hie d i 1 ut ion
after reaction to
form calcium chlo-
ride; should check
w/local authorities
'9,28
28
30
A large amount will 10,19
s i nk to bottom of
water body so dredg-
ing may be required
0.125
0.25
0.125
0.25
-------
TABLE 22. (continued)
Hazardous
Chemi cal
Carbon
Di sul fide
Amenable to
Biological Trmt.
at Municipal STR
no
Treatment Scheme
Backwash
m — -|F| — -@-~
Carbin £ CS2
Backwash
Treatment
Speci f i cat ions
C: 10-100 H/lt
sol . mat 1 .
Prov .
Limit
Comments Reference mg/1
Dredging of the 19.33 1.0
bottom of the
water body may
be needed
Chlordane
Chlorine
Chloro-
benzene
Solids
£ Chlordane
., - ,,.
Na Bisulfite
then S=
When reduced
and diluted
when diluted
Chloroform when
Backwash
1
,•*•
C: '00-300 «//'
so' • ^atl.
Add H2SO^ f.o pH 2-3;
add Ma bisulfite
until small or no
chlorine residual;
neutral ize to pH 7
C : 10-100 F/#
so'- niat'-
C: 10-100 S/?
sol. mat 1.
Dredging of the
bottom may be
necessary
Carbon can be
used for low
concentration
of C
Sedimentation £
dredging of water
bottom may be
necessary
19
19,
19,33
10,19
0.025
0.15
17-5
6.0
Chlorosu)-
fonic acid
when
neutralized
Ca(OH)
2 rLO
Add Ca (Oll)2 slowly
to pll 7; dTlute i f
necessary
Dissociates to
/, 5 HC1 in
H2SO
water and is explo-
sive; diIute to
meet Cl" and S0i,=
discharge levels
0.05
or 250
as SOi,
Cl
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt.
Chemical at Municipal STP Treatment Scheme
H2SO') H2S(\
Ammonium no - Ca(£H)2 ,
Bichromate ^\ f(~*\ *(V^ *-() *\ 1
NaBisulfite
1 N !• 1 1 Y [a
\Y/ i — r
T
Ca(OH)2
Treatment
Spec if I cat ions
Add H2SOi, to pH 2-3/
add bisulfite to
large ORP change or
yellow to green color
react 10 min/add
Ca(OH)2 to pH 8-5
settle/neutralize to
pH 7/filter/IX in
weekly acidic resin/
neutralize with lime
to pH 7
Comments Reference
Both chrome and 19
ammonia must be
removed/alum or
polyelectrolyte
may be necessary
to aid settl ing
of Cr (OH)-,
j
Prov.
Liiri t
mg/l
0.05
as Cr
0.01
as NH
J
Ammonium
Chromate
See Ammonium
Bichromate
19
0.05
as Cr
0.01
as NH,
HC1 then
Na bisulfite
Calcium
Chromate
. CKOH)
Adjust pH to 2-3; add
bisulfite until color
changes to green or a
large color change;
add 11me to pH 8-9/
allow to settle/
neutralIze
Alum or polymer -nay 10,19,
be required to 20,24,
Improve the settling/ 13,23
filtration after pre-
cipitation may allow
removal of fines 6
suspended Cr(OH)j
0.05
as Cr
-------
TABLE 22, (continued)
Hazardous
Chemical
Chromic
Acetate
Amenable to
Biological Trmt .
at Municipal STP
no
Treatment Scheme
Ca(OH)2 HCI
Treatment
Specifications
Adjust pH to 8-9
with slaked 1 ime/
Comments Reference
Alum or poly- 19,20
electrolyte may
Prov.
Limi t
mg/1
0.05
as Cr
Chromic
Acid
Chromic
Sulfate
Chromous
Chloride
Chromyl
Chloride
' Cr(OH)3
See Chromic Acetate
*>ee Chromic Acetate
Ca(OH)2
-^ /*^° i
1>r"^
H,SO
Ca
Out
al low to settle/
f i Iter if needed/
neutral ize
Add Ca(OH). to
pH 8,5/settle
Add H SO, to pH
2-3; add\isulfite
to large ORP change
or color yellow to
green; react 10 min/
add lime/s.oda ash to
pH 8-9/settle/add
HCI to pH 7
be requI red to
improve the
settling/f11tratIon
after precipitation
may a I low removal of
fines t suspended
Cr(OH)3
Chromous will oxidize
to chromic so
siudqe will be
mixture of chromous
£ chromic hydroxide/
use alum or poly-
electrolyte to aid
settlinq
Dilution may be
necessary to reduce
CL concentration
13,20
19,20
19
19,20
0.05
as Cr
0.05
as Cr
0.05
as Cr
0.05
as Cr
250
as Cl
-------
TABLE 22. (continued)
Hazardous
Chemical
Li thium
Bichromate
Li thi urn
Chromate
Potass ium
Bichromate
Potassium
Chromate
Sod i urn
Bichromate
Sodium
Chromate
Strontium
Chromate
Amenable to
Biological Trmt.
at Municipal STP Treatment Scheme
H?SOJ, then HC 1
Bisulfite . * . HO
— X*N Jk Jk i2
( S^ — "vy — -00 — -(y) — *-••
T IT ^"^
* *
no See Lithium Bichromate
no See Chromyl Chloride
no See Calcium Chromate
no See Calcium Chromate
no See Chromyl Chlorate
no na Bisulfite Ca(OH) Ca(OH)
1 1 1
Treatment
Specifications Comments
Add H.SO, to pH Check acceptable
2-3; add bisulfite lithium levels
to large ORP change
or color yel low to
green/react 10 mins/
add Ca(OH) to pH 8-9/
settle neutralize with
HC1 to pH 7
Check acceptable
1 i thium levels
Add H SO, to pH 2-3 Remove Chromate
add bisulfite until sludge or decant
F.ov.
Limit
Reference mg/1
19, 2k 0.05
as Cr
19.2A 0.05
as Cr
19,2i( 0.05
as Cr
19, 2k 0.05
as Cr
19, 2k 0.05
as Cr
19, 2k 0.05
as Cr
19, 2k, 26 0.05
as Cr
( s
turns green or large
ORP change/ add Ca(OH)2
to pH 8.5/settle/add
more 1ime to pH 10/
settle/discharge
supernatant before
second lime addition
check acceptable
strontium levels
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt.
Chemical at Municipal STP
Zinc no
Bichromate
Treatment Scheme
Coba1tous
Bromide
M.
I H20
HCI
Ca(OH)2 H20
Treatment
Spec!fications
Add H2SOj, to pH 2-3/
add bisulfite until
color turns green or
large ORP change/
add 50/50 1ime/soda
ash to pH 7.5-8.5
settle Zn(OH)2 and
chrome sludge
Add 1ime to pH 8-8.5/
settle/neutralize to
pH 7 with HCI
Comments
Alum may aid in
settling floe
Reference
10,19,20
Dilution may be
needed to meet the
bromide discharge
requi rements/Both
cobaltic & cobaltous
hydroxide are insolu-
ble at pH 8-8.5
'9,26
0.05
as Cr
0.05
as Co
Coba1tous
Fluoride
Ca(Oh)
Add 1ime to pH 8-8.5/
settle/allow to react
2k hours/neutralize
and discharge
A long holding time
is needed to reduce
F concentration
19,33
0.05
as Co
Cobaltous
Formate
Cobaltous
Sulfamate
See Cobaltous Bromide
HOC1 HCI
Ca(OH),
Add HOC1 to residual
then add Ca(OH)2 to
pH 8.5/settle CaSO,
add HCI to pH 7/filter/
IX on weakly acidic
resin/neutral ize to
pH 7
Dilute to meet 19,26 0.05
acceptable formate as Co
concentrations
Sulfamate is con- 19,24,26 0.05
verted to sulfuric as Co
acid and ammonia
when oxidized
-------
TABLE 22. (continued)
Hazardous
Chemical
Cupric
Acetate
Amenable to
Biological Trmt.
at Municipal STP
When di lute and
neutral ized
Treatment Scheme
Ca(OH)2
Backwash H,SO,
Treatment
Specifications
Add lime to pH 9.5
al low to settle/
Comments Reference
Carbon may be bene- 19,24,33
ficial in low ranges
Prov.
Limi t
mg/l
1.0
as Cu
fi1ter for more
sol ids removal/
neutralIze to pH 7
otherwise precipita-
tion is effective/
ammonia must be re-
moved prior to treat-
ment
Cupric
Aceto-
arsenite
Ca(OH)2
H2,0
Add Ca(OH)2 to pH 8
and allow insoluble
compound to precipi-
tate
Dilute if necessary;
initial material is
insoluble in water
so dredging may be
necessary
19,
0.05
as As
Cupric
Chloride
Cupric
Formate
When dilute and
neutralized
When dilute and
neutralized
See Cupric Acetate
See Cupric Acetate
Dilute to meet ac- 19,24,33 1.0
ceptable Cl- concen. as Cu
Formate is degradea- 19,24,33 1-0
ble in STP as Cu
Cupric
Glycinate
Cupric
Lactate
Cupric
Ni trate
Backwash H,0
When dilute and
neutralized
When dilute and
neutralized
Backwash
Same as Cupric Acetate
C: 10-100 #/# sol.
material
C: 10-100 #/# sol.
material
Glycinate forms a 19,24 1.0
complex which should as Cu
be adsorbed/untested
treatment scheme
Lactate also com- 19,24,26 1.0
plexes/untested as Cu
treatment scheme
Dilute nitrate to 19,24,26 1.0
below acceptable as Cu
discharge level
-------
TABLE 22. (continued)
Hazardous
Chemical
Cupric
Oxalate
Cupric
Subacetate
Cupr i c
Sulfate
Cupric
Sulfate,
Ammonia ted
Cupric
Tartrate
Cuprous
Bromide
Coumaphos
Cresol
Amenable to
Biological Trmt.
at Municipal STP Treatment Scheme
When dilute and See Cupric Glycinate
neutral i zed
When dilute and See Copper Acetate
neutral ized
When dilute and See Copper Acetate
neutral ized
Backwash
1 HCI 1 1 c^9HLH[3'X!)~l
When dilute and (T) •j"p~) — •T^l »
neutralized T" I |^
Backwash
no j air Ca(°H)2 H2S04
Backwash H Q
When diluted jt J_^ 1 ,2
When diluted (?) rTTI »m
Treatment
Specifications
Add HCI to PH ?/
filter exchange/add
Ca(OH) to PH 9.5/
settle/neutral ize/
di lute
C: 10-100 #/# sol .
material
Add ai r 70% of max.
residual/add lime to
pH 9.5/fi Iter
neutral ize to pH 7
C: 100-300 #/# sol .
material
C: 1-10 f/» sol.
material
Prov.
Limit
Comments Reference mg/1
Forms complex/ 19, 2k, 33 1.0
untested treatment as Cu
scheme
19,24,26 1.0
as Cu
19,2l»,26 1.0
as Cu
Decomposes to NH, 19,24,26 1.0
and CuSO, as Cu
Forms complex/un- 23 1.0
tested treatment as Cu
scheme
Coagulant may be 30 1.0
needed to increase as Cu
settl ing rate
10,19 0.001
Backwash
-------
TABLE 22. (continued)
un
Amenable to
Hazardous Biological Trmt.
Treatment
Chemical at Municipal STP Treatment Scheme Specifications Comments Reference
Barium When acclimated „
Cyanide (cyanate only) ( S) — ~fo) — ^PV*Tf
T T Y n
I NadH Na^SOi,
1 then HOC1
Backwash
Calcium If acclimated then H4d I
Cyanide ("s^^S ^\
r X ^^/
NaOH
£ HOC! H_
Hydrogen If acclimated i 2
Cyanide _ J:
Acid) *" ^~
HC1
j Add NaOH to pH 8.5 Coagulant may be 2Q
l-^Aiy-^ and then HOC1 to a needed to increase
r-1 W residual/react 1 hr/ settling rate use
add Na2SO/4 sulfate test to
excess SO/./settle/ establish dosage
filter/and neutralize for Na.SO./shorter
t u 7 react Ion -eq 10 min
P at pH of 10-11 will
create cyanates
(much less toxic)
Add NaOH to pH 8.5 A shorter reaction 10,19,20
^ then add HOC 1 to 10% time at pH of 10-11
excess/react 1 hr/ dosage will allow
neutralize to pH 7 reduction to cyanate
for discharge to STP
SO,
**H Add NaOH to pH 8-8.5 Do not allow pH to 10,19,20
? then add HOC1 to a drop below neutral
n — L. residual/add 10% XS or NH, will be formed
HOC 1 /react 1 hr/neu- /add Targe excess
tralize w/H SO, prior NOC1 to avoid the
to discharge liberation of toxic
cyanogen chloride
Potassium If acclimated See Calcium Cyanide 10,19,20
Cyan i de
Sodium If acclimated See Calcium Cyanide 10,19,20
Cyan! de
Zinc Cyanide no HOP 1 ^
Add 1 ime to pH 8. Sand The CN must be 1Q 2Q
then add excess HOC! removed prior to .'
Prov.
Limi t
mg/l
0.01
as CN
0.01
as CN
0.01
as CN
0.01
as CN
0.01
as CN
0.01
as CN
settle/filter if nee.
neutralIze
keep pH up unt iI CN
is removed to prevent
HCN generation/filtra-
tion at end may help
ef fIuent qua!i ty
-------
TABLE 22. (continued)
un
Amenable to
Hazardous Biological Trmt. Treatment
Chemici.1 at Municipal STP Treatment Scheme Specifications
Prov.
Limit
Comments Reference mg/1
NaOH H-sQr
HOC1 H20
Cyanogen if acclimated 1 , i Add NaOH to pH 8-8.5 6 Activated carbon 10,19, 0.01
Chloride (?) *(p\ I-{N) '> 10^ excess HOCl/allow may also be used 20 as CN
— v^/~"v-x to react 1 hr/neutral ize/ if necessary
dilute if necessary
Backwash
(.yclohexane When dl luted 1 jl J- C : 10- 100 #/# sol .
Backwash
2,'t-D (acid) no ($\_ -J~F~|— 4Ar— » c: 35-100 #/# sol.
^-' ~ — 1 ' — ' matl.
Backwash
' ° BSter "° (4)_^JF|_JA| . C: 35-100 #/# sol.
^ * — 1 1 — ' matl.
Backwash
DalaP°n n° (j) — J~F(— J~A] — » C: 100-300 #/# sol.
mat 1 .
DDT no ^7)— »TT|— «4~AJ • C: 100-300 #/# sol.
Backwash
Dlcamba no , , C: 35-100 #/# sol.
Skim eye lohexane 10,19 52.5
off surface and
then adsorb remainder
on carbon
Dissolves slowly 10,19 0.5
so dredge from
bottom
Dissolves slowly 10,19 0.5
so dredge from
the bottom
19
10,19 0.05
Dredge if possible 30
then adsorb soluble
portion on carbon
30
matl-
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt. Treatment
Chemical at Municipal STP Treatment Scheme Specifications
nichloheoil no Backwash f . ioo-300 ft/ff sol
X?*\ i\ p j , | jft 1 K mat 1 .
Dichlone no i JL I C: 100-300 #/# sol.
CD —
-------
TABLE 22. (continued)
Hazardous
Chemical
Amenable To
Biological Trmt.
at Municipal STP Treatment Scheme
Treatment
Specifications
Prov.
Limit
Comments Reference mg/1
Dinitrophenol
i. uackjvasn i
(j) - •[?]— »{A| — »•
mat).
VI
Oiquat
Disulfoton
Diuron
Backwash
Backwash
Dodecylbenzene- When diluted r~
sulfonlc acid ( e ) ,| p I j ^
Dodecylbenzene- When diluted
sulfonic acid,
calcium salt
C: 100-300 #/# sol.
matl.
C: 100-300 #/# sol.
matl.
C: 100-300 #/# sol.
matl.
Backwash
Neutralization
may be needed
C: 10-35 #/# sol.
matl .
C: 10-35 #/# sol.
matl.
Very little will
dissolve unless a
wetting agent is
available so skimming
or dredging may be
necessary
19,30
30
10,30
Dilute if needed or
remove Ca separately
23
Dodecyl benzene- When diluted
sulfonlc acid
isopropanolamine
salts
Backwash
C: 10-35 #/# sol.
matl.
23
Dodecyl benzene- When diluted ,•*•> .rri JT1
sulfonic acid 'e^n-LrTAI
sulfonic acid
sodi urn sal t
C: 10-35 #/# sol.
matl.
23
-------
TABLE 22. (continued)
Amenable To
Hazardous Biological Trmt.
Chemical at Municipal STP
Dodecyl benzene- When diluted
sulfonic acid,
trie thanol ami ne
salt
Treatment Scheme
Backwash
Treatment
Speci f icat ions
C: 10-35 #/# sol.
mat 1 .
Comments
Reference
23
Prov.
Limi t
mg/1
Dursban
Endrin
H 0
Backwash 2
so) ids to landf i 1 1
C: 100-300 it/tt
sol . mat 1 .
C: 100-300 /?/#
sol . mat) .
Di lution may be
requl red prior to
discharge-check to
determine if skimming
or dredging is needed.
30
I0>19
0.005
vn
Endosulfan
Backwash
solids & endosulfan
C: 100-300 ///#
sol. matl.
sinks — so dredging
may be needed—also
dilute treated efflu-
ent i f requi red.
10
Ethion
Ethyl benzene When dilute
Bacjv^l, |
— HH3 — -
sol ids
di lution f.
C: 100-300 tt/tt
sol. matl.
C: 10-100 #/# sol.
mat 1.
Skimming may be
sufficient, however
carbon will provide
further poli shing.
30
12,19 22
-------
TABLE 22. (continued)
Amenable To
Hazardous Biological Trmt
Chemical at Municipal STP Treatment Scheme
Ethyl ene When di lute
Diamine
NaOH Backwash
JL JL I I
( s V- -(CR)— -pr"!^"") — "•
7
Treatment
Prov.
Limi t
Specifications Comments Reference mg/1
C: 35-100 #/# sol.
matl . Add NaOH to
make alkal ine (pH 8-
8.5). before adsor-
ption
10 1.27
Aluminum
Fluoride
sol Ids solids Al (OH),
CaF-CaCO, J
Add lime to pH II
let stand overnight
(24 hrs) then add
HC1 to pH 7 settle
to remove Al (OH).
discharge.
Complete fluoride
removal requires
2k hours/add coagu-
lant to aid settling
of Al(OH),
10,19
0.6-1 .7
as F
ui
oo
Ammon i um
Bi fluoride
When neutral- Backwash
ized and
di luted
JL
(vi>-
s~~\.
•\N)~ '
HCI
J-
•{_£
Ca(OH)
Na,~~
Add HCI to pH II
filter/ion ex-
change add 50/50
Ca(OH) /Na CO- to
PH 11/react 21, hrs/
decant/neutralize
to pH 7.
Fluoride requires
2k hrs. for ppt as
CaF-CaC03
19,28
0.6-1.7
as F
Ammonium When neutralized See Ammonium Bifluoride
Fluoride and diluted
10,19
0.6-1.7
as F
Hydrofluoric If
Acid diluted
Ca(OH)
sol ids
sol ids
Add 50/50 mixture
of soda ash/1ime
unti I pH 11; allow
to stand overnight/
f i 1ter/neutralize
with HCI.
Fluoride requires
2k hrs. for ppt as
CaF-CaCO
19,28
0.01
-------
TABLE 22. (continued)
vn
VD
Amenable To
Hazardous Biological Trmt.
Chemical at Municipal STP
Sodium If di luted
Bif luoride
Sodium If di luted
Fluoride
Stannus If di luted
Fluoride
Treatment Scheme
Ca(OH)2 HC1
AUSOi, 1 V
/7\ r/p\ 4~r~| r/n\ *>
^o/ *^~Y "1 — 1 \-J
*
Same as Sodium Bifluoride
Na2COj &
CaTOH]2 HC1
I I H,°
Treatment
Spec! f ications
Lime to pH 1 I/add
alum to a good floe;
al low to react for
24 hrs/f i Iter/neutra-
1 i ze £ di lute.
Add 50/50 mixture
of 1 ime and soda
Prov.
Limit
Comments Reference mg/1
Fluoride requires 19,28 0.6-1.
24 hr reaction time as F
19,28 0.6-1.
as F
Alum may be used 19,28 0.6-1.
to improve the as F
1
7
7
Formaldehyde When
dilute
Backwash
ash to PH ' I/allow
to stand 21, hrs/
f i Iter/neutral ize
and di lute.
C: 35-100 #/# sol.
mat 1 .
settling rate.
31
0.15
Formic Acid When
dilute
CarH'2.H20
Add lime to pH 7.
Sodium bicarbonate 31 0.45
can also be used.
Fumaric When dilute
Acid
NaOH or
solids 6 fumaric acid
C: 35-100 #/# sol.
mat I. Neutralize
if necessary
Remove fumaric acid
w/solIds-bottom of
water body may require
dredging; Anion ex-
changers may also be
used.
31
-------
TABLE 22. (continued)
Amenable To
Hazardous Biological Trmt.
Chemical at Municipal STP Treatment Scheme
Backwash
Furfural When dilute (^) — »j~FJ — .|7~| ••
sol ids
Backwash
Guthion When dilute (S ) — •fr]— nM~*"
Solids
Backwash
r r |
Heptachlor no (S) — "pT" *T^I — *~
solids
Na2CO, £
Ca(OH)2
Hydrochloric When neu- [
Acid tralized ("51 -AT) - out
r
Hydroxyl- When dilute HOC1 Ca(OH)2
amine .1
Treatment
Spec! fi cat ions
C: 10-100 tf/tt sol.
matl.
C: 100-300 #/#
sol . matl .
C: 100-300 #/#
sol. matl.
Add 50/50 lime
soda ash to pH 7
Oxidize by slowly
adding weak HOC I/
neutralize by add-
Pro V.
Limi t
Comments Reference mg/1
Dredge, pump or 10,19,20 1.0
vacuum the undissolved
portion from bottom.
Dredge pump or 10,19 0.01
vacuum undissolved
portion from bottom-
hydrolyzes in acid or
cold alkali
Vacuum or pump 10,19,37 0.025
undissolved portion
from bottom/ remove
heptachlor w/solids;
very little dissolves.
Stirring is needed; 10,19 0.35
do not add NaOH 250
because resulting mg/p
reaction is quite as Cl-
violent/check to meet
acceptable Cl levels
Add only dilute HOC1 10 0. 5
to prevent violent as
reaction/forms HNO. HNd
ing Ca(OH)7 to
pH 7
to be neutralized
-------
TABLE 22. (continued)
Hazardous
Chemical
Ferric
Ammon i urn
Citrate
Ferric
Ammonium
Oxalate
Ferric
Chloride
Ferric
Fluoride
Ferric
Nitrate
Ferric
Sulfate
Amenable to
Biological Trmt. Treatment
at Municipal STP Treatment Scheme Specifications
Uhpn neutral- Backwash
ized and dilute 1 Ca(OH)2
(^^$HJ}-
V/hcn neutral i Backwash
When neutral j
ized and ^ • 2 j. 1
dilute (jV^p)— @—\f_
When Ca(OH)2
dilute ,_ JL
rr
sol ids Fe{OH)
__ -, Ca(OH) A*H/I r*(cm\ tr\ r»n
1 HO 6"7/Ppt Fe7f ilter/
.— L, JL 1 2 exchange neutralize
-03--0-1- to PH 7
T^fr\u\ ftHH r-»(OH\ tn nH *>/
I i settle/reduce pH 6-7
TJlV{N>-* w/HCl/ppt Fe/f ilter
J 1 iW exchange/neutr to pH 7
M n
2 Add 1 ime to about
j pH 7 and ppt Fe(OH3)
neutral ize if
necessary
3
When fafnHl /u n Add ' ime to PH 7/
dilute C-(OH)7 ,M rn * V al low Fe (OH), to
1 Fa2LU3 1 settle/add more lime/
( S J-WpV-^/pWTUOi) soda ash to pH 1 I/
- ^-S ^> L_l V-y sett)e 2J< hrs/fi,ter/
neutral Ize
When dilute Ca'°H>2
(7^A_.
sol ids Fe(OH)
H 0
2 Add 1 ime to pH 7 and
/~~\ j ppt Fe(OH)j/neutral ize
"VV to pH 7 with HCI or
1 ime if necessary
3
When dilute See Ferric Chloride
Comments Reference
Di lute may be 19*
needed for
citrate
The first ppt 19*
should remove
oxalate
Ferric hydroxide is '0,'9
least soluble at pH
7 so this pH is
recommended
Alum may improve 19,20,28
settl ing after
second 1 Ime add i-
tion/Fluorlde re-
quire 2k hrs for
removal
Di lute nitrate to 10,19
acceptable level
10, 19, 2*i
Prov.
Limit
mg/1
0.03
as Fe
0.03
as Fe
0.03
as Fe
0.05
as Fe
0.03
as Fe
0.03
as Fe
-------
TABLE 22. (continued)
Hazardous
Chemical
Ferrous
Ammonium
Amenable to
Biological Trmt.
at Municipal STP
When oxidized/ I
neutralized/ 1 a
Treatment
Treatment Scheme Specifications
Backwash
,r Ca(OH)2
Ca(OH) Aerate until no
. 2 H20 Fe"1"2 remained/add
Comments Reference
Oxidation
ferrous to
changes 19, 24*
ferric/
Prov.
Limit
mg/1
0.03
as Fe
exchange/neutral Ize
to pH 7
should occur
rapidly
Ferrous
Chloride
When dilute
pHadj. Ca(OH)2
6 air HCI H.O
Backwash
Adjust pH to 7.5
wi th IIme or acid/
allow to aerate until
no ferrous Iron exists/
add lime and adjust pH
to 7/react/settle/
filter/discharge
The lime should
be added to achieve
sufficient floccula-
tion/polyelectrolyte
may be needed
10,19,20
0.03
as Fe
Ferrous
Sulfate
When dilute
Isoprene When dilute
See Ferrous Chloride
scum
Backwash
C: 10-100 #/# sol.
mat!.
The sulfate ion 10,19,20 0.03
may result in as Fe
large amounts of
calcium sulfate In
the sludge
Skim undlssolved 10,19 110
off top with booms
and adsorbent
Kelthane When dilute
I I I
Backwash
C: 100-300 #/# sol.
matl.
Di lut ion may be
required prior to
discharge, check
bottom to see If
dredginq Is required
10,30
-------
TABLE 22. (continued)
Hazardous
Chemical
Amenable to
Biological Trmt.
at Municipal STP Treatment Scheme
Treatment
Spec! f ications
Prov.
Limit
Comments Refence mg/1
Kepone
no
C: 100-300 i/ff sol,
mat!.
Kepone is extremely
toxic, dilution
may be needed prior
to discharge
Lead
Acetate
2.
I. Add Ca{OH) to pH
8-9/ppt filter/
neutralize to pH
7 i f needed
!. C 10-100 #/# sol.
mat!.
Use Carbon as a
polishing step/
NajCOj may also
be used
19,20*
0.05
as Pb
Ca(OH>2
ON
Lead no
Arsenate
Lead no
Chloride
Lead no
Fluoraborate
Lead no
Fluoride
r tnu\ r r i n * u
f7y_/p\ VpN ,rpi /jk j^ 8.5/settle/add more
•lead 5 solids and FeClj to form
f loc/settle/f liter/
neutralize if needed
FL^i^ch Add Ca(OH), to pH
J Ca(OH). | H20 8,5/ppt lead filter/
^*-^ f**^ _[-[ \ discharge. Use
vl-'*AL/ "1^1 carbon as a polishing
step
Ca(OH)2 KCI ^ Add Ca(OH). to pH 8.5
x-^ .1^ JL . — . 'A ppt/decant/add KCI
LL/~*VPJ)~H\Py~H'r 1 — ^ to ppt/filter/dis-
charge
Ca(OH).,
Ca(O.H) HO Add ^a'^^'2 to pH
If 2 i ? 8. 5/al low to settle/
(l)-1^p)--/p)--J"T}— 1— decant 6 add 1 ime to
1 S~^ pH ll/settle 2k hrs/
Backwash filter/discharge
Vacuum, dredge or 10,19,20
pump off bottom. *
Both Arsenic £
lead wi 1 1 be re-
moved
Dredge, vacuum or 10,19,20
pump undissolved *
portion from
bottom
Can precipitate \3,2^*
some fluoraborate
with KCI untested
scheme
Dredge, vacuum or 19,20,28
pump undissolved por-
tion from the bottom.
Fluoride requires 2^
hrs to remove
0.05
as Pb
0.05
as As
0.05
as Pb
0.05
as Pb
0.05
as Pb
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt. Treatment
Chemical at Municipal STP Treatment Scheme Specifications Comments Reference
Lead no See Lead Chloride 10,19,28
Iodide
Lead no See Lead Chloride Dilute so nitrate 10,19,28
Nitrate cone, reaches accep-
table levels/dredge,
pump, etc. undis-
solved portion from
bottom
Lead no See Lead Chloride 10,19,28
S tea rate
Lead no See Lead Chloride Pump vacuum or 10,19,28
Sulfate dredge undissolved
portion and solids
from bottom
Backwash
Lead no J. 1^
Tetraacetate ^J.^"*!""!]""'
,rh , C: 10-100 #/# sol. Dredge undissolved 31
' — ' mtl. portion from
bottom
Lead no See Lead Chloride Dilute cyanate 10,19,20
Thlocyanate lf needed
Lead no See Lead Chloride 10,19,20
Thiosulfate
Backwash
L«ad "o 1 Ca(OH)2
Tungstate JL i
0__(py.
t\2u
If Add 1 Ime to pH 7-8/ Dredge, pump or 26
•ITI — ** filter to remove vacuum undissolved *
Prov.
Limit
mg/1
0.05
as Pb
0.05
as Pb
0.05
as Pb
0.05
as Pb
0.05
as Pb
0.05
as Pb
0.05
as Pb
0.05
as Pb
fines/settling is
necessary
from bottom
-------
TABLE 22. (continued)
Hazardous
Chemical
Amenable to
Biological Trmt.
at Municipal STP
Treatment Scheme
Treatment
Specifications
Prov.
Limit
Comments Reference mg/l
Backwash
Llndane
C: 100-300 H/tt sol.
mtl .
Dredge, pump or
vacuum undissolved
portion of sol Ids
from bottom
10
Malathion
Backwash
C: 100-300 #/# sol.
mat 1 .
Dredge, pump or
vacuum undissolved
portion from
bottom
10
Malelc
Acid
After neutrali
zation
Backwash
C: 1-10 #/# sol.
mat I .
Dredge bottom as
fast as possible
19* 0.05
vn
Maleic
Anhydride
After neutral i-
za t i on
NaHCO
STP
eacKwa s n
1 . Add NaHC03 to pH 7/
dilute; send to STP
2. C: 1-10 #/# sol. matl.
Either option is
acceptable depend-
ing on avallable
chemicals &
discharge point
10,19 0.05
Mercuric
Acetate
Raise pH to 7-8 with
NaOH/add NazS to a S°
residual/fi1ter/
adsorb & aerate to
5 tng/l DO residual
Take care not
to evolve H.S
at low pH
19,20,24 0.005
as Hg
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt.
Chemical at Municipal STP Treatment Scheme
Mercuric no 1 oacKwasn i i
Cyanide \_r^ ,/->. ,H~I .r^l
S — iT IT — L—_ J
NaOH NaOH
S= HOCI ^ ^
"^\_/
T
HC1
Mercuric no See Mercuric Acetate
Nitrate
Mercuric no See Mercuric Acetate
Sulfate
Mercuric no See Mercuric Acetate
Thiocyanate (most will settle)
NaOH
Na-S ai r
Mercurous no 2. .
Nitrate , -, A A I — I r
Prov.
Treatment Limit
Specifications Comments Reference mg/1
Raise pH to 8 with CN- can be reacted 19,20,24 0.005
NaOH/add H.S to S= to cyanates if pH as Hg
— i residua I/ react 5 min/ is raised to 10-1 I/
sett le, remove sludge/ reaction time is re-
adjust pH to 8.5 add duced to 10 min.
_| HOCI to residual + Dilute cyanates if
10% excess/react 1 necessary.
hr./f i Iter/adsorb/
neutralize. C: 1-10
#/# sol . mat!.
19,20,24 0.005
as Hg
19,20,24 0.005
as Hg
Sedimentation is 19,20,24 0.005
required/can dilute as Hg
if necessary
1. Add NaOH to pH 6-8/ If option 2 is used, 19,24 0.005
— . add Na.S to residual mercury and mercuric as Hg
( SV— -(P)— \0>H F MA |— - aerate'to mercuric sulf ide wi 1 1 be
•^ ^ — ' ^—S 1 1 L^
Backwash
NaOH/Na2S
state/filter/adsorb. present In sludge
C; 1-10 #/# sol.
matl .
2. Add NaOH to pH J-6/
add Na.S/let stand
until no mercurous
-------
TABLE 22. (continued)
Hazardous
Chemical
Methoxychlor
Methyl
mercaptan
Amenable to
Biological Trmt.
at Municipal STP
no
After chlorine
reduction (treat-
ment scheme #2)
Treatment Scheme
Backwash
( S)-JT] — JA] — *
'sol ids
Backwash
US>-J~FUJ~A|_*
Treatment
Specifications
C: JOO-300 #/# sol.
matl .
1. C: 35-100 #/# sol.
matl .
Prov.
Limit
Comments Reference mg/1
Dredge, pump or 10
vacuum undissolved
portion from bottom
Be sure to elimi- 10,19
nate all ignition
sources
2. Add HOC1 to C]
HC1 or NaOH residual/then neu-
to STP tralize to pH 7 if
necessary
Methyl When dilute
methacrylate
.scum
w/compd Backwash
C: 10-35 #/# sol.
matl.
Skim the si !ck
off surface of
material
10,19
20.5
Methyl When dilute into
Parathion effective acti-
vated sludge
system
Backwash
C: 100-300 ///# sol.
matl .
Vacuum, dredge or
pump undissolved
portion from
bottom
10,19
0.001
Mevinphos
(Phosdrin)
sol ids £ Mevinohos
C: 100-300 #/# sol.
matl.
Check bottom £
remove any in-
soluble mat' 1
nO
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt. Treatment
Chemical at Municipal STP Treatment Scheme Specifications Comments
Mi rex no fsV-H M — A A \~ * C: 100-300 #/# sol. May require di
1 mat 1 tion prior to
1 charqe
Monoethyla- When dilute Ca(OH) H 0 MaY be able to
mine or reduced X /^~\^ i \^ some compounds
( S )-~»(CRj-»j F]-*JA |-*- surface. Cat!
T Backwash T T ch^"9e "" be
tions may requ
di lution
Prov.
Limi t
Reference mg/l
lu-
dis-
sklm 10,19 0.9
from
on ex-
used on
1 solu-
ire
OO
Monomethyla- When dilute
mine
Backwash
solids CafOHU
Raise pH to 8 with
lime/filter. C:
10-100 #/# so), matl.
May also be used for
exchange
10,19
0.9
Ma led
no
Backwash
C: 100-300 #/# sol.
matl.
30
Naphthalene When dilute
Backwash
C: 10-35 #/# sol.
matl.
Dredge, vacuum
or pump undlssolved
port ion t sol Ids
from bottom
10,19
2.5
-------
TABLE 22. (continued)
Hazardous
Chemical
Amenable to
Biological Trmt.
Treatment
at Municipal STP Treatment Scheme Specifications
Comments Reference
Prov.
Limit
mg/l
Backwash
Napthenic
acid
When neutral- NaOH
i zed i i.
©— •*0y~'
Add NaOH to pH 11
i— H p*-| __ filter/adsorb on
1 FM Ar~" carbon. C: 10-35
19
-
solidsT& Napthenic acic #/# sol. matl.
Nickel
Ammonium
Sulfate
Bac kwa s h
no 1 Ca(OH)2 HC1
{ Su-^j^/Nj-JTl.
\ r*\rr~\£S^]J_r
sol ids sol ids NI (OH)2
Ca(OH), HO Add Ca(OH) to pH
I | 10/ppt Ni/add HC1
J~JX~1 WfS X. to pH 7/filter/
^-^ ^~J neutralize to pH 7
May requi re di lu-
tion to reach SO, 19,24
discharge levels. A
Make sure ammonia
not present in high
amounts/lime treat-
0.05
as Ni
Backwash
Nickel
Chloride
Backwash
2.
Add Na CO, to pH
8-8.5/all6w to
settle/filter
Add 1ime to pH
lO/allow to settle/
fiIter/neutralize
in lower nickel
levels
19,24
*
0.05
as Ni
Nickel
Formate
Na
Add soda ash to pH 8-
8.5/allow to settle/
filter/neutralize to
pH 7
Determine accepta-
ble formate dis-
charge level/ion ex-
change or carbon ad-
sorption may be
needed
19,24
0.05
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt.
Chemical at Municipal STP Treatment Scheme
NIckel Ca(OH), HCI
Hydroxide no V. 2 T
Nickel no See Nickel Chloride
Nitrate
Nickel no See Nickel Chloride
Sulfate
Ca(OH)2
Nitric When neutral- Na2C03 H,O
^v-^-L
Sot Ids
Ra«-bw»ch
Nitro- Not to all JT "l \
benzene systems/only CD~*j F }— -^ A| ».
some J^ ^~^
solids 6 Nitrobenzene
Nitrogen After neutral 1-
Dioxide zatlon and di- Ca(OH)2
lutlon _ J |2
Treatment
Specifications
Add time to pH IO/
allow to settle/
filter/neutralize
with HCI
Add 50/50 soda ash to
slaked 1 [me until
pH 7/dllute/dlscharge
C: 10-100 #/# sol.
raatl.
Add Ca(OH). to pH 7-8
dilute with water
Comments Reference
A coagulant may 19. 20, 24
aid settl Ing/neu-
tralization with
acid may be neces-
sary first
19,2*»
Check discharge 19,24
cone, for sul fates
Dilution to reduce 10,19
nitrate concentration
Dredge, pump or 10,19
vacuum insoluble *
portion from
bottom
Beware of flash fire 28
Self-contained breath- *
ing apparatus mandatory/
Prov.
Limit
mg/1
0.05
as Ni
0.05
as Ni
0.05
as Ni
0.25
0.25
-
K
solids (Treat In situ
when possible)
lime addition forms ni-
trates and nitrates
reqr. dilution
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt.
Chemical at Municipal STP Treatment Scheme
Backwash
Nitrophenol no 1 [ \
^s~) *fn »[ A 1 »-
V-x l_l T — T
solids 6 Nitrophenol
Para- When dilute Barkuach
formaldehyde i \ \
(iHiH^H
Para^hlnn Uhon Hil,.,-. If Backwash
activated sludge JL 1 1
process is accli- Qy"*Tn — *\ AJ — *"
ma ted J|
Backwash
Pentachloro- no 1 [ |
phenol /g\ rfrl JA! *-
V_/ 1 — II — 1
I
Backwash
Phenol No unless very 1 1 ]
dilute A. r-U J-.
Treatment
Specifications
C: 10-35 #/# sol.
mat).
C: 10-35 #/# sol.
matt.
C: 100-300 #/# sol .
matt .
C: 100-300 ft/it sol.
mat! .
C: 1-10 #/# sol.
mat).
Comments Reference
Dredge, pump or 18,19
vacuum insoluble
portion from
bottom
10,19
Dredge, pump or 10,19
vacuum undissolved
portion from bottom
Dredge, pump or 10,19
vacuum undissolved
portion from bottom/
Ion exchange may be
used if avai table
Dredge undissolved 10,19
portion from bottom
Prov.
Limit
mg/l
0.01
0.15
0.005
0.25
0.001
Phosgene
no
Ca(OH)2 H20
«!' VJ) ^~
(Treat In situ when possible)
Add Ca(OH). to pH 7-8/
dilute with H20
Extreme caution
needed/use self-
contained breathing
apparatus/toxic gas
0.02
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt.
Chemical at Municipal STP Treatment Scheme
Phosphoric When neutralized
Acid Ca(0>i)2 ,HC1
( "s ^ — ^p\__J~f~L_»/7)
._. V_y 1 l \_y
T i
i i
BaTkwa sTT
Phosphorus no Place under water or
wet sand and remove
from scene to
manufacturer
Phosphorus If neutralized ^Jackwajh
Oxychloride S diluted iCa(OH), , HC1
I i
( s )— »(pV-»4Vi »CN) •
v— \-S ( 1 \^>
Backwash
1 Ca/OH\ HOC1 HC1
Phosphorus If neutralized It2 JL jL
Pentasulfide £ diluted ( s V-^>)_J71_-^o)-H/N)— -
Specifications
Add 1 ime to pH 1 I/
al low to sett 1 e (an
anionic polymer may
help)/f i 1 ter if needed/
neutra 1 ize to pH 7
Add 1 ime to pH 1 I/
(check to see if CaCl2
removes more P)/settle/
(use anionic polymer
if needed )/f i 1 ter i f
necessary/neutralize to
pH J with HC1
Add 1 ime to pH 1 I/
settle/filter if"
Comments Reference
The volume of sludge
may be excessive so
eval uat ion of this
aspect from bench
tests is required/
use CaCl2 to reduce
volume and a i r
removal
Will s ink but
caution must be
taken to avoid
contact with air or
risk spontaneous
igni t ion
This compound decom- 10,20,
poses to HC1 and 32
phosphoric acid/
large volumes of
sludges may be pro-
duced so this factor
must be considered--
use CaCl2 with Ca(OH)2
to reduce sludge
volume and remove P
Decomposes to form 30
H2S and phosphoric *
Prov.
Limit
mg/1
0.005
0.35
0.05
necessary/oxidize with
HOC1 until residual
exists/neutralize with
HC1
acid so immediately
raise the pH to avoid
evolution of toxic H2S
Phosphorus If neutralized See Phosphorus
Trichloride 5 diluted Oxychloride
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt.
Chemical at Municipal STP
Polychlorinated no
Biphenyl s
Treatment Scheme
Backwash u r,
III "2
Cs)^M~*rM — ^
Specifications
C : 100-300 #/# sol.
mat 1 .
Comments Reference
Dredge, vacuum or 10
pump undlssolved
port ion and sol ids
from bottom
Prov.
Limit
mg/l
0.025.
to
0.05
Potass ium
Hydroxide
When neutralized
and diluted
Potassium When reduced
Permanganate & diluted
Acetic Acid
Propionic
acid
when d i lute
£ neutralized
(S
NaOH
Backwash
Add acetic acid to Cation exchange 10,19
PH 7 may also be used.
Care must be taken
to avoid excessive
heat buiIdup
Adjust pH to 9-10 with Natural reducing '9,22
NaOH and add bisulfite agent will most likely
to large ORP change/ reduce the perman-
react 10 min/flocculate ganate/ carbon may
t settle/filter if be used as reducer
needed/neutralize to also
pH 7
Add NajCO, to pH 7/
fi1ter/adsorb
C: 10-100 #/» sol.
matl.
Not a problem in sea 10,lg
water because ppt with
CaCl,
0.10
0.05
as Mn
1.25
Propionic When dilute See Propionic Acid
Anhydride 6 neutralized
C: 10-100 #/# sol.
matl .
Wi11 not dissolve
in salt water
10
1.25
P ropy 1
A 1 coho I
When dilute
Backwash
H20
C: 10-100 #/# sol.
matl.
Carbon may be in-
effective so ex-
tensive dilution
may be reguired
10,19
25
-------
TABLE 22, (continued)
Hazardous
Chemical
Amenable to
Biological Trmt.
at Municipal STP
Treatment Scheme
Treatment
Spec! f icat ions
Prov.
Limit
Comments Reference mg/1
Backwash
Pyrethrins
C: 100-300 #/# sol
matl.
10,30
Quinol ine
(S
Backwash
C: 10-35 #/# sol.
matl.
Pump or vacuum
undissolved por-
tion from bottom/
wi 1 1 only dissolve
slowly
10,30
Resorcinol
Backwash
C: 1-10 #/# sot.
mat
Is very soluble
so al 1 water
should be treated
10,30
Selenium
Oxide
air
Backr,
H2*°l>
acid to pH 6.5, Take care to avoid
add Na,S until
slight excess settle/
filter if needed/
oxidize to remove S
Filter/exchange for
Se removal/neutralize
evolution of H,S/
Use ion exchange
if media is avai la-
ble or If desired
19,20,2'*
*
0.01
as Se
Sod i um
Selentte
See Selenium oxide
19,20,24
*
0.01
as Se
-------
TABLE 22. (continued)
Hazardous
Chemical
Amenable to
Biological Trrot.
at Municipal STP Treatment Scheme
Treatment
Spec! f ications
Prov.
Limit
Comments Reference mg/1
Sodium
When neutral I zed
(N
H2° HAC
IS'
sol ids
If on land, cover with
oi 1 and haul. Protect
from contact with water
or air.
Add acetic acid to
pH 7/dredge
Dilute prior to
neutralization/
is dissolved in
water as NaOH
10,19 0.1
as NaOH
Sodium After reduced
Bisulfite with hypochlorite
Add soda ash to pH 10/
then add HOC! to a
chlorine residual/
react 2 hrs/neutralize
with HCI and discharge
Be sure chlorine
residual is low
10,19,28
Sodium When reduced
Hydrosulfide
air
H,0
Na2C03
j—(J)—(o)—L.
Add Na2CO, to pH 7-
a!r to 70? max.
DO level
Remove any sol ids
to land f i 11
10,19
Sodium When neutra-
Hydroxide lized
acet ic acid or
dil,ute H2SOi| or
HCI Add acid to pH 7/
discharge
Be careful not to
create strong
react ion
10,19,28
O.I
as NaOH
Sod i urn
Hypochlor i te
After reduction
£ neutralizat ion
bisulfite
Add bisulfi te and
acidify with H-SO^
to pH 2-3/add soda
ash to ppt Ca sulfate/
pH 10/neutralize
with HCI
19,28
0.125
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt.
Chemical at Municipal STP
Sodium If neutralized
methytate
Sodium If oxidized
Nitrite
Sodium If di luted
Phosphate
(dibasic)
Sodium If di luted
Phosphate
(monobasic)
Sodium If diluted
Phosphate
(trlbasic)
Sodium If oxidized
Sulfide
Prov.
Treatment Limit
Treatment Scheme Specifications Comments Reference mg/1
HAc
"2U Add acetic acid Whenever possible 0.1
-. JL 1 to pH 7 /dilute send to STP/other- as NaOH
(S) — *\NJ *—• jf needed wise dilute/can give
| off CH^/also forms
Sol Ids NaOH in water
See Sodium Bisulfite
Ca(OH)2 HCI Add lime to pH 117 38 -
^^^ Ji j[ allow to settle
(TVWpV- 4~T] fc/N) — » (use anionic polymer
V j
-------
TABLE 22. (continued)
Hazardous
Chemical
Amenable To
Biological Trmt.
at Municipal STP
Treatment Scheme
Treatment
Specifications
Prov.
Limit
Comments Reference mg/1
Backwash
Strychnine
Styrene
If diluted
skim
SV-JFJ—JAl
sol Ids 6 strychnine
Backwash
C: 100-300 #/# sol.
matt .
C: 10-100
mat! .
sol.
Dredge, pump, or
vacuum undissolved
portion from
bottom
Skim surface of
water body
10
10,19
21
Sulfuric
Acid
If neutralized
NaoCO
Add 50/50 mixture
of 1 ime and soda ash
to pH 7/settle
calcium sulf i te
sludge if needed/
d ischarge
Be careful not to
create violent
reaction by too
fast base add it ion
10'19
°'°5
Sulfur If neutralized
Monochloride
Ca (OH)->
I H2°
Add 50/50 mixture soda
ash and 1 ime to pH 7/
allow any sludge to
settle
Will decompose in
water to sulfuric
acid/may fume to
H2S so take special
precaut ions
10,19
2,^,5-T
(acid)
Backwash
No
sol IBs s 2,4,5-T
C: 100-300 #/# sol.
mat).
Dredge, pump or
vacuum undissolved
portion from bottom
30
2,'t,5-T
No
See 2A5-T acid
30
-------
TABLE 22. (continued)
00
Amenable To
Hazardous Biological Trmt. Treatment
Chemical at Municipal STP Treatment Scheme Specifications
Comments Reference
Prov.
Limit
mg/1
Backwash
TDE no i
(ODD) (SV-H
r
Backwash
dnW
Ca(OH)2
Tetraethyl no /'~Y_«/Y_.j —
Pyrophosphate ' Uj/ *v£/""!_F.
1 !
Backwash
» skim
Toluene When dilute /-k < — i
CS>H M —
II C: 100-300 #/# sol.
j~j — J"A] ^ matl.
Ca(OH)? HC1 Adsorb C: 10-35 #/#
1 i sol. mat). Add Ca
^}*(2H5)~~*" (OH)2 t0 pH 8'5/PPt
lead neutral ize to
pH 7 if needed.
HC1
iA^_] Add Ca(OH)2 to pH 11
• ^-^ settle/filter if
necessary/neutral ize
to pH 7/dilute
rm . C: 10-100 #/# sol.
L-t-l matl.
loxapnene no j T | C: 10-100 #/# sol.
(sy*[T| — »[A] .. matl.
remove toxaphene
S sol ids
Trirhlnrfon no ,- Backwash ,nn.™n *///—,
Dredge, pump or 10,19
vacuum undissolved
portion from
bottom
Dredge, pump or 10,19,33
vacuum undissolved
portion from bottom
Carbon may be
effective
Forms phosphates and -
methanol when hy-
dro! yzed untested
theoretical only
Skim off surface 10,19
of water body
Dredge, vacuum or 30
pump undissolved
port ion from
bottom
0.05
0.05
18.75
matl.
any undissolved
portion from the
bottom/usually wi 1
be dissolved
30
-------
TABLE 22. (continued)
Amenable To
Hazardous Biological Trmt. Treatment
Chemical at Municipal STP Treatment Scheme Specifications
Backwash
Trichloro- no 1 1 1 C: 10-100 #/# sol.
phenol /y\ Jr"L JA! matl.
tr Icnlorophenol
Ca(OH)2
Triethyla- When dilute "?,^/*'A_J — LJ — | _ Add ''me to PH 9.
mine ' V~*'v:RJ""H F \~*\ ^ 1 " then run through
„ . , | filter. C: 35-100
Backwash „ .„ . .
HI It SOl . Hid 1 I .
Backwash
Trimethyla- When dilute 1 T 1 C: 35-100 #/# sol.
mine ( § \ »| r 1 J A I • ma 1 1 .
Uranium no Ca(OH),. . • C- 35-100 ttfff sol
Peroxide JL /AN —1— _^^ matl.
Uranyl no See Uranium Peroxide
Acetate
Uranyl no See Uranium Peroxide
Nitrate
Uranyl no See Uranium Peroxide
Sulfate
Prov.
Limit
Comments Reference mg/1
Dredge, vacuum or 23
pump undlssolved
portion from
bottom
Solubility is 19 5.0
reduced at high
temperatures
Add Ca(OH) to pH 10,19 5.0
9/f 1 Iter if neces-
sary/neutral ize to
pH 7
Uranium perioxide is 26*
a strong oxidizing
agent/insoluble at
pH 8/10
Uranyl acetate can 26*
also be precipitated
as a phosphate
26*
26*
-------
TABLE 22. (continued)
Hazardous
Chemical
Vandium
Pentoxide
Amenable To
Biological Trmt.
at Municipal STP
Treatment Scheme
Treatment
Specifications
Add Ca^OH^2 to pH 8>5/
Add Fe+3
with air/d! lute
26,39*
Vinyl
Acetate
di lute
C: 10-35 #/# sol.
of f f rom
water body;
1ight may cause
polymerization
to sol id so
dredging may
be required
10,19 1.5
Xylene When dilute
skim Backwash
C: 10-35 #/# sol.
mat!.
Skim surface of
water body
23
Xylenol When dilute
.Backwash
H-0
C: 10-100 #/# sol.
matl.
Skim surface of
water body
10,19 0.001
Zectran
ackwash
C: '00-300 #/# sol.
matl>
30
-------
TABLE 22. (continued)
Amenable To
Hazardous Biological Trmt.
Chemical at Municipal STP Treatment Scheme
MCI
Zinc no fc>\k/"F} •["?! •O'VJI~
Acetate Vl/^y' <-J ^V7
Ca(dH)2 '
a2 3
Treatment
Specifications
Add 50/50 mixture of
soda ash and 1 ime to
pH 7.5-8.5; allow to
settle/filter if
needed/neutralize to
pH 7
Comments
Check to assure
discharge of
acetate is
acceptable
Prov.
Limit
Reference mg/1
10,19,20, 5.0
24 as Zn
Na0CO,
Zinc
Ammonium
Chloride
Settle/fi1ter/exchange
add 50/50 Iime/soda ash
to pH 7.5-8.5/settle
filter if needed/neu-
tralize if necessary
Ammonia must be
removed first
24,26* 5.0
as Zn
oo
Zinc
Borate
See Zinc Acetate
10,19,20,
24,26
5.0
as Zn
Zinc
B romi de
See Zinc Acetate
10,19,20
24,26
5.0
as Zn
Zinc Carbonate
Add Iime to pH
7.5-8.5/settle/
filter is needed/
neutralize to pH 7
10,19,20, 5.0
24,26 as Zn
Zinc
Chloride
See Zinc Acetate
10,19,20, 5.0
24,26 as Zn
-------
TABLE 22. (continued)
Amenable To
Hazardous Biological Trmt.
Chemical at Municipal STP
Zinc no
Fluoride
Treatment
Ca^OH?2
, 7i _/b> m
I 5_l »(F J »| F |
Scheme
Na2CO,
Ca(OH}2
.X.
nrl — «/"M\. 1
Treatment
Specifications
Add soda ash to pH
7.5-8.5/settle/filter
if needed/add addi-
tional soda ash/ lime
to pH 1 I/settle 24 hrs/
neutral ize to oH 7
Comments Reference
F requires 24 hrs 10,20,24
for removal at
high pH
Prov.
Limit
mg/1
5.0
as Zn
Zinc
Formate
See Zinc Acetate
10,19,20, 5.0
24 as Zn
Z i nc
Hydrosulf ite
CO
N5
Oxidize with HOC) to
residual/add Ca(OH)2
to pH 7-5-8.5/filter
if needed
Oxidize to remove
hydrosulfite
10,19,20, 5.0
24,26* as Zn
Zinc
Nitrate
See Zinc Acetate
10,19,20, 5-0
24 as Zn
Z i nc
Phenol -
sulfamate
no
Backwash
Adsorb C: 10-100
#/#, Add Ca(OH),
to pH 7.5-8.5
Precipitation wi 11
remove any excess
Zn
19,24* 5.0
as Zn
Ca(OH)
Zinc
Phosphide
Add Ca(OH)2 to pH
7-5-8.5/settle
Do not lower pH or
phosphine will be
formed
19,24*
5.0
as Zn
-------
TABLE 22. (continued)
Hazardous
Chemical
Zinc
Potassium
Chromate
Amenable To
Biological Trmt.
at Municipal STP
no
Treatment Scheme
H,SOi. then
Bisulfite Ca(OH)2
x-. JL JL HaO
^^W-*®-^
Treatment
Specifications
Settle to remove
ZnCrO^/ Add f^SO^
to pH 2-3, then bisul-
fite to large ORP or
color change/add
Ca(OH)2 to pH 8/settle/
discharge
Comments Reference
Color changes from 19,2^*
ye 1 low .to green
Most ZnCrO^ will be
removed early
Prov.
Limit
mg/1 '
5.0
as Zn
Zinc
Si licof luoride
Ca(OH) Ca(OH)
Add Ca(OH)_ to pH
8.57 react
First lime dosage
destroys silico-
fluoride complex
test rxn careful ly
19, 2 A*
5.0
as Zn
CO
Vjo
Z i nc
Sulfate
See Zinc Acetate
Add additional 1 ime
to pH 11/settle 2k
hours/di lute
5-0
as Zn
Z i rcon i urn
Acetate
Ca(OH)
Add lime to pH 107
al low to settle,
filter if necessary,
neutral ize with HC1
Check discharge
limit for Zirconium
26*
Z i rcon i urn
Potassium
Fluoride
H0
Settle and dilute
A very stable
complex/no other
treatment
recommended
26*
Z i rcon i urn
Nitrate
See Zirconium Acetate
26*
-------
TABLE 22. (continued)
Amenable to
Hazardous Biological Trmt.
Chemical at Municipal STP
Treatment Scheme
Treatment
Specifications
Comments
Reference
Prov.
Limit
mg/1
Zirconium
Oxychloride
Backwash
HoO
CaoH}2
Add Ca(OH), to pH ?/
settle/filter/dilute
May need polyelec-
trolyte to aid
settling
20*
Zirconium
Sulfate
Zirconium
Tetrachloride
See Zirconium
Acetate
See Zirconium
Oxychloride
oo
-------
5.0-CHAPTER 5 - SAFETY CONSIDERATIONS AND PROCESS DESIGN
5.1 GENERAL
5.1.1 Approach
The total section involving field implementation of treatment processes is
very lengthy and for presentation in this Manual it has been divided into
three sections. This first section presents sources of already constructed
equipment for use in treating hazardous material spills, it also emphasizes
the critical safety considerations evident in dealing with hazardous material
spills and presents methods for developing the needed process design cri-
teria. The next chapter (6) provides stepwise direction for individual de-
sign and construction of each of the five types of treatment processes. The
final chapter (7) outlines needed information regarding process components
such as tanks, pumps etc. and treatment chemicals. Step by step procedures
are presented using cross references throughout the chapters to reduce repe-
tition as much as possible.
Due to the complexity of treating hazardous spills and the need to make
the manual as compact as possible, much desirable but not absolutely
necessary information has been excluded. This procedure should not
hamper the user but rather challenge him and his technical advisors to
build from the basics presented here a system to suit the specific con-
ditions and limitations with which he is faced.
5.1.2 Operation Design
It is essential that the OSC and other technical spill personnel be
familiar with this Manual prior to use. Certain specific information
sources have been left open and must be completed by the OSC prior to
actual use of the manual. A good example is the location of local
sources of materials, components, services, and supplies necessary to
implement the field processes.
It is recommended that the duties at the site of the spill be divided
into three distinct categories. A process engineer or director would be
concerned with the process and the chemistry of the treatment. A main-
tenance engineer would oversee construction and then perform the
necessary surveillance of the equipment to assure correct mechanical
operat ion.
Finally, a separate safety director would be appointed whose only concern
would be to attempt to provide safe working conditions in a hazardous
situation. The people must work together closely to create a safe and
effective working environment.
5.1.3 Forma^
These chapters have been structurtsJ to use various cross references in order
185
-------
to minimize repetition. The general approach of the three chapters is shown
in Figure 37- The various chapter references are shown with the action
guiding scheme. The close association with Chapter 4 is apparent. Per-
formance of bench tests is not always mandatory since some processes don t
require this procedure. However, when needed, it must be done immediately.
The chapters are based on a two-fold philosophy. The first is scaleup of
the bench test results (where applicable) to allow design of a full size
unit. The second, and more critical aspect of the design, is a limiting
factor approach to establishing a process flow rate. In order to correctly
evaluate the systems calculations are made and then the entire system should
be mapped out on paper. Once this paper treatment system is "constructed",
it can be evaluated in terms of the limiting factors in the specific spill
situation. The procedure for applying this approach is given In subsection
5
-------
ACT!ON
DECS S ION
TO
TREAT
1
r
CHOICE OF
FLOW
SCHEME
fr.
7
PERFORMANCE
OF
BENCH TESTS
CHAPTER 6
ESTABLISH
PROCESS
FLOW RATE
CHAPTER 5
ORDER
MATERIALS
CHAPTER 7
CONSTRUCT
CHAPTER 6
OPERATE AND
MAINTAIN
EQUIPMENT
CHAPTER 6
Figure 37- Stepwtse use of chapters fr, 5, 6 and 7-
187
-------
5.2 AVAILABLE EQUIPMENT SOURCES
Once it has been established that the spill must be treated using an on-site
but off-stream system, it is necessary to construct the needed process units.
Prior to following the instructions for improvising a treatment system as
presented in Chapter 6, it is recommended that the spill coordinator investi-
gate the possibility of using preconstructed system components. The OSC or
other authorized personnel should determine the availability of equipment
to be used in hazardous material spill cleanup. Table 23 presents a list
of some of the available sources of equipment throughout the country. Prior
to a spill situation, it would be desirable for the OSC to be familiar with
these sources and other local suppliers so that upon the occurrence of a
spill, the availability of preconstructed equipment can be determined
rapidly.
5.3 SAFETY PRECAUTIONS
5.3.1 Approach
Safety procedures are critical when working with hazardous materials
and even more so when operating an improvised treatment system. It is
critical to judiciously guard the safety of those people on the treatment
site to prevent creating a disaster out of the hazard. The operators
must be alerted to possible dangers and potentially hazardous situations
by a specific person at the scene. Since most people will be concerned
with designing, constructing, or operating the system, it seems best to
choose a separate individual whose only responsibility would be safety on
the treatment site. This person, hereafter termed the Safety Director,
would have direct responsibility for all aspects of safety.
Among the safety director's duties are obtainment of various safety
equipment, the transfer of information regarding the hazard of the situation,
the specificaUon of the level and type of protective clothing needed for
each position, operation and person*and policing of the area to insure that
safety standards are followed. It is the safety director's duty to work
directly with the process and maintenance engineers to incorporate safety
considerations into the entire system. Therefore considerable diligence
and tact are necessary to do an effective job.
5.3.2 General Duties
The safety director has many responsibilities for adapting a spill site
into a safe working area. These are summarized in Figure 38. In the
beginning of the set-up the safety director must approve the layout of
the system and the chemical and fuel storage facilities. Special instruc-
tions for storage are available in many references and these should be
consulted. The safety director should also restrict access to certain
areas of the treatment system by roping them off. Specific restricted
areas should include chemical feed systems and any inground tanks.
Warning signs should also be placed in especially hazardous areas.
188
-------
TABLE 23. PORTABLE TREATMENT EQUIPMENT SOURCES
(Used chemical process equipment suppliers)
San Francisco
Machinery and Equipment Corp.
P.O. Box 3132C
San Francisco, California 94119
Phone: 415-467-3400
Houston
Dynaquip, Inc.
1143 Brittmore
Houston, Texas 77043
Phone: 713-467-5500
Petro-Power, Inc.
6436 Rupley Circle
Houston, Texas 77087
Phone: 713-644-8271
Chicago
Aaron Equipment Co.
9301 W. Bernice Street
Schi1ler Park, I 11inoi s
Phone: 312-678-1500
60176
A-1 Equipment 6 Chemical Co.
57 East 21st Street
Chicago, I 11inois 60616
Phone: 312-842-2200
Indeck Power Equipment Co.
1075 Noel Avenue
Wheeling, Illinois 60090
Phone: 312-541-8300
Loeb Equipment Supply Co.
4131 South State Street
Chicago, Illinois 60609
Phone: 312-548-4131
Union Standard Equipment
163-167 N. May Street
Chicago, Illinois 60607
Phone: 312-421-1111
Cleveland
Arnold Equipment Co.
5055 Richmond Road
Cleveland, Ohio 44146
Phone: 216-831-8485
Cleveland (Continued)
C.P.R. Machinery & Equipment Co.
5061 Richmond Road
Cleveland, Ohio 44146
Phone: 216-464-8590
Federal Equipment Co.
8200 Bessemer Avenue
Cleveland, Ohio 44127
Phone: 216-271-3500
International Power Machinery Co,
834CE Terminal Tower
Cleveland, Ohio 44113
Phone: 216-621-9514
Process Equipment Trading Co.
1250 St. George Street
East Liverpool, Ohio 43920
Phone: 216-385-2400
New York
Brill Equi pment Co.
35-63 labez Street
Newark, New Jersey 07105
Phone: 201-589-7420
George Equipment Co.
27 Haynes Avenue
Newark, New Jersey 07114
Phone: 201-242-9000
HSP Equipment Co., Inc.
14 Skyline Drive, Box 368
Montville, New Jersey 07045
Phone: 201-335-9770
Keith Machinery Co.
34 Gear Avenue
Lindenhurst, New York
Phone: 516-884-1200
11757
Perry Equipment Co., Inc.
Box C
Hainesport, New Jersey 08036
Phone: 609-267-1600
189
-------
SET-UP
Establishment of layout
Approval of storage facilities
Restriction of access
Placement of warning signs
Creating of first aid station
MATERIALS
Obtaining clean water for washing and safety uses
Ordering safety equipment
Listing emergency numbers and instructions
Providing safe lighting
COOPERATION WITH LOCAL AUTHORITIES
Aid police in restricting access
Show fire department hazard of situation
POLICE THE OPERATION (enforce safety regulations)
IMPRESS UPON PARTICIPANTS THE HAZARD OF THE SITUATION
Specific hazards of the contaminant
Specific hazards of the operation
Figure 38. Summary of a safety director's responsibilit
tes
190
-------
While chemicals and media are being ordered, the safety director should
obtain the necessary safety equipment and clothing. These materials are
available from various suppliers. A discussion of these devices is
included at the end of this chapter. The safety director should also
obtain a source of clean water for use in washing and for emergency
shower and eyewash systems. It must be stressed that all workers are
dealing with a hazardous substance and should wash thoroughly prior to
eating or touching anything. Finally, It is critical that the safety
director instruct each person performing a specific operation with re-
gard to ?ts hazards and the level and type of protective clothing
needed for the task.
In addition to these duties, the safety director must set up a protected
safety or first aid station with a cot, blanket and first aid kit.
Emergency numbers, the location of hospitals and telephone numbers of
doctors in the area should also be obtained. In addition, lighting should
be provided on the site if nighttime operation is expected.
The safety director should also work with local author51ies--police,
civil defense and fire department--to establish procedures for both
emergency and normal operating situations. Police may be able to restrict
access of unauthorized persons to the site, while both civil defense and
fire department officers should inspect the system prior to the develop-
ment of any emergency situation. The safety director should be familiar
with the hazards of the specific contaminant being treated. He must have
knowledge of antidotes or special safety procedures to insure that
adequate precautions are taken. This information must then be conveyed
both to local emergency authorities and to the people working at the site.
Once the system is operating, the safety director must Inspect the area
regularly, and check to make, sure the system and the people are working
safely. AH treatment equipment should be inspected as should the protec-
tive clothing worn by operators.
However, it Is more Important for the safety director to impress upon the
operators of the equipment the importance of system safety. The various
situations which present specific hazards should be explained and the
possible affects made known to the workers. If this is done effectively,
safety will be a concern of all people on the spill site and accidents can
be avoided or minimized.
5.3.3 Specific Operat?ng_and Ma In tenance Haza rds
There are many inherent safety problems which arise when a jury-rigged
system 5s operated. The following sections indicate some of the situa-
tions which require special attention. Once on the scene, a safety direc-
tor should be able to notice many more. It is necessary to warn the person
performing the task of the specific hazards involved and help him to mini-
mize them.
5.3.3.1 Desludging - The desludging operation involves transfer of a con-
191
-------
centrated and highly contaminated sludge. In general, the job Is messy and
difficult. All personnel Involved in this task should wear protective
clothing and eye protection as specified by the safety director and avoid
unnecessary contact with the sludge.
5.3.3.2 Hose Repositioning - Moving hoses may be a necessary task and it
may be difficult to do without showering the area (and people) with contami-
nated liquid since hoses can easily get loose. When hoses are to be moved,
the pump feeding them should be shut off and for extra safety the person
moving the hose should wear protective clothing and eye protection, speci-
fied by the Safety director.
5.3.3.3 Tank Patching - When tanks require repair, this must usually be
done from the inside of the tank and therefore may involve direct contact
with the contaminant. Two people should be involved In the operation and
both should be equipped with specified protective clothing and goggles. One
person must enter the drawn-down tank while the other can stay outside to
assist in any manner necessary. However, extreme caution is needed to
avoid falling since the tank bottom liner may be quite slippery.
5.3.3. *> Pump Handling - Pumps must be watched at all times, so flow can be
shut off immediately to avoid downstream problems. When hoses on pumps are
removed, It is necessary to fully relieve the pressure which builds up at
the pump to avoid blow back of the wastewater. The pump operator should
be equipped with protective clothing and eye protection to avoid Injury
from this situation. The raw flow pump is also very difficult to set up
and handle, so operators should be protected and take special precautions.
5.3.3.5 Hoses and Fittings - Another problem involves slippage between
hoses and fittings which occurs during operation. To minimize the problem
a maintenance director can check these systems throughout the day and re-
tighten them as necessary. Anyone In the vicinity should be protected to
avoid contact with the contaminant in case the hose breaks loose.
5.3.3.6 Chemical Feed System - The handling of treatment chemicals and the
chemical feed system is a very dangerous operation In a jury-rigged system.
Specific cautions and problems are Indicated in Chapter 7. however certain
general rules should be followed. The chemicals should not be touched
under any circumstances and a respirator should be used if dust is present.
Eye protection, gloves and rubber aprons or specified protective clothing
are necessary for anyone operating the feed pump or mixing chemicals. As
stated previously, the area should be restricted and access granted only
to those wearing proper safety equipment. The hoses for chemical systems
must be well supported so that they don't loosen and spray chemicals on
unprotected individuals. In addition, hoses, fittings and pumps should be
inspected frequently and any leak fixed Immediately. These chemicals can
present a personal hazard equal to or greater than exposure to the contami-
nated liquid because of the high concentrations involved. Therefore, the
safety director must stress this fact to all people concerned with treatment
and strictly enforce the safety regulations.
192
-------
5.3.4 Commercially Available Safety Equipment
5.3.4.1 General - The safety equipment previously referred to will be
described in this section. This equipment Is commercially available and a
number of vendors are given at the end of this discussion. The needed
safety materials should be ordered and kept on hand by the OSC, by responsi-
ble agencies such as police and fire departments, and by contractors involved
in hazardous material spills cleanup.
5.3.-A.2... Testing Equipment - Testing of the air is often advisable at the
scene of the spill to determine if a combustible, toxic or oxygen deficient
atmosphere exists. While there are varying degrees of sophistication,,
portable instruments which would be of the most use include:
1. Universal tester - tests for a wide range of toxic gases.
2. Combustible gas indicator - measures combustible gases or vapors.
3. Oxygen indicator - tests for concentration of oxygen.
5.3.4.3 Protective Clothmg - Protective clothing available includes res-
piratory devices, suits, gloves, hoods, shoes and boots. A comprehensive
Inventory of much of this equipment is available in the U.S. GPO Publica-
tion "A Survey of Personnel Protective Equipment and Respiratory Apparata
for Use by Coast Guard Personnel in Response to Discharges of Hazardous
Chemicals" (NTIS ADA - 010-110)(42). In addition to listing of available
safety equipment, a prototype of the Coast Guard fully protective suit is
included. This document should be obtained for use by the safety director
at the spill site. Respiratory devices include atmosphere supplying
breathing apparatus, gas masks and other types of respirators (dust, mist
or paint spray, etc.). Breathing apparatus have their own source of air
or oxygen rather than attempting to purify and use the ambient, contaminated
air. Breathing apparatus are the safest and recommended type of respiratory
protection and should be used unless it 5s confirmed that the contaminant
can be removed by a filter or canister. A breathing apparatus provides
general protection against toxic gases and oxygen deficiency- The most
commonly used breathing apparatus is the self-contained air mask. A cylin-
der of air is carried on the back of the user and is supplied on demand.
Exhaled air is exhausted to the surrounding atmosphere.
Gas masks provide protection against a specific hazard when equipped with
the appropriate chemical-sorbent canister. Canisters are available to pro-
tect against low concentrations of acid gases, organic vapors, carbon
monoxide, ammonia, and chlorine. In no case should a canister gas mask be
used if there Is a chance that the concentrations may exceed the sorbent
limit or that an oxygen deficiency may exist.
The protective suits (thought of as completely enclosing the wearer) provide
trie Maximum protection against a hazardous environment. There is no suit
commercially available which is resistant to all hazardous chemicals. The
Coast Guard is developing a uutyl rubber maximum protection suit and the
U.S. EPA is developing a lightweight butyl rubber suit. Once the hazard
is known, however, appropriate clothing usually can be selected from what
193
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Is commercially available. In most cases this will be acid resistant cloth-
Ing, i.e., fabric coated with vinyl, butyl, or neoprene rubber. A typical
commercially available suit consists of a neck-to-toe, one piece coverall
and a separate hood. Air Is supplied to the suit from an outside source.
Less restrictive garments are also available but provide less protection.
Coated gloves are available to protect against various chemicals. Hard
hats should be worn if there Is a danger of falling objects or low-clearance
bump hazards. Hard toe boots and shoes should be standard items, however,
It must be stressed that protective clothing Is only effective when the
Identity of the spill Is known and when the clothing Is properly used. If
the specific hazard is not known, a fully protective suit may not provide
long term protection for working In the spill vicinity. The hazard associ-
ated with improper use of protective clothing is obvious.
5..3«A. ** Eye Protection - Eye protection In the form of safety glasses
or goggles should be required of everyone on the site of a spill clean-
up. Unlike some street glasses, safety glasses have lenses that are
impact and shock resistant. Side-shields or goggles are recommended
if corrosive chemicals are to be handled or pumped.
5.3.^.5 Skin Protection - skin creams are available for protection
against specific types of irritants. These irritants include acids,
alkalies, tar, and cooling and cutting oils.
5.3.^.6 First Aid Equipment - A first aid kit should be kept at the
site of the spill cleanup. A portable resuscitator may also be in order
depending on the hazards involved.
5.3./K 7 Vendors - Safety equipment is available from the following
vendors (among others) :
Mine Safety Appliances Company
^00 Penn Center Boulevard
Pittsburgh, Pa. 15235
Environmental Tectonics Corp.
k James Way
County Line Industrial Park
Southampton, Pa. 18966
215-355-9100
Additional equipment may be found locally by checking the Yellow Pages
under Safety Equipment and Clothing.
19**
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SYSTEM DESIGN CRITERIA
General
Once it has been established that the spill must be treated on site in
an offstream treatment system, many considerations must follow. The
first design step is to establish the process flow rate of liquid through
the treatment system before further design can be started. Various
factors affect the flow rate including time, site considerations, material
availability, manpower requirements and the characteristics of the con-
taminated liquid itself. It is best to consider each spill situation
individually and evaluate which factors limit flow in that spill occur-
rence. This section presents the various factors and then applies ex-
amples to indicate how the site and material problems can be solved
using the built-in flexibility of a parallel batch system. However
the section does not attempt to judge a situation, but rather to present
circumstances which may occur to make the OSC aware of these limiting
factors.
S.k.2 Limiting Factors in System Design
Many factors are used to establish the maximum possible flow rate through
a specific treatment system. Some of the variables are outlined in
Figure 39. They have been divided into six general headings and each
of these will be discussed in the following sections.
5.^.2.1 Time - For many spill situations, time is a critical factor for
various reasons. In some circumstances there is immediate danger or a
change in weather conditions will create a more severe problem by
spreading the spill, so treatment must be completed before the next
precipitation event. Possibly, the men on site are only available for
a limited amount of time or the local authorities insist the spill must
be cleaned by a certain time. In any event, once a time is established,
and the volume of spill is known, then a process flow rate can be cal-
culated.
5.^.2.2 Si te Con si de rat i ons - A new set of factors is introduced when
the site is being considered. If the spilled material is extremely
hazardous, a treatment site near the spill may be dangerous and the
available pumping capacity may be insufficient to convey the contaminated
liquid to a treatment system located a far distance from the spill it-
self. Another consideration is accessibility to the spill site by
vehicular traffic (i.e. trucks) to allow equipment, supplies and manpower
to reach the site. Other important considerations involve the amount of
firm, fiat and clear area available for construction of tanks and other
large area requiring equipment. Modifications of the site with earth
moving equipment or fill may be needed to allow a sufficient area to
provide the required capacity of the treatment system.
Other problems involved in site considerations are the proximity to
residences and roads. Residential interference may create problems when
195
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TIME:
Immediate Danger
Meteorological Conditions
Local Political Considerations
SITE CONSIDERATIONS:
Safe Proximity to the Spill
Accessibility by Vehicles
Clear Area
Flat Area
Firm Ground
Number of Setups Requires
Proximity to Residences
Restriction to Civilian Vehicular Traffic
MATERIAL AVAILABILITY:
Sufficient Tankage
Sufficient Pump Transfer Capacity
Media Availability
Chemical Availability
Special Equipment Availability
PROCESS RESTRICTIONS:
Long Detention Time in Sedimentation
Difficulty in DesJudging
Long Contact Times Required in Columns
Large Volumes of Sludge Obtained
MANPOWER LIMITATIONS;
Sufficient Skilled Labor for Construction
Sufficient Labor for Operation
MISCELLANEOUS PROBLEMS;
Degree of Contaminant
Available Hauling Capacity
Figure 39. Limiting factors In system design.
196
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2k hour per day operation is desirable or nearby roads may require
special police or DOT provisions. Finally if the spill extends over a
long distance, the number of times the treatment system nust be set up
has to be considered. A central but relatively remote location may be
absolutely necessary to avoid reconstructing the treatment system at
another si te.
5.k.2.3 Materia 1 Ava11abi 11 ty - Once a flow rate has been estimated, the
amoun t of cons t r uc t i on ma te rI a1s and chemicals needed to meet this goal
can be calculated. At this point, various parts of a treatment scheme
may completely limit the flow through rate. These requirements are also
directly related to the contaminated liquid treatment characteristics.
In general, the most common limiting factor will be the availability
of sufficient tankage to handle the spill. This required tank volume
will also directly affect the area needed for treatment as discussed
previously. Another consideration is the availability of sufficient
pump capacity for transfer from the liquid source through the treatment
processes and back to a receiving body of water together with the require-
ments of the chemical feed system and desludging operations.
In some situations, special equipment is needed to allow the safe handling
of corrosive material and this special supply may be limiting. Finally,
the availability of treatment chemicals and column media may affect the
overall flow rate. However, It must be remembered that partial orders
can be shipped before the complete order to reduce this problem.
5.k.2.k Process Restrictions - The treatabllity of the contaminated
liquid will also affect the design of the treatment system. A slow
settling liquid will require more tankage. Also a sludge which is bulky
or difficult to remove or pump from the tank will increase the number of
needed tanks. The specific hazardous material being removed may need
longer column contact time (especially for carbon) or may require removal
to a higher degree. Finally, the characteristics of the cpntaminated
liquid may result in a large volume of bulky sludge to be removed daily.
5.**.2.5 Manpower Limitations - There are two types of general labor re-
quired, although both functions can be filled by the same people. The
first is the labor required for construction of the treatment plant within
a short period of time. Local contractors can generally provide assistance
in this area. The other manpower requirement is for the actual operation
of the treatment system. Table 2k summarizes the approximate manpower
needed for each operation on a per shift basis. However, prudent
scheduling or a reduced working day may reduce the number needed. In
general, based on 8-10 hr./day of work, each pump requires at least one
person to operate it and column operation may need more manpower. Super-
visory manpower must also be included and should include at least 3
people: process director, maintenance director and safety director plus
some personnel to aid in process control functions.
197
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Table 24. MANPOWER REQUIREMENTS FOR
VARIOUS UNIT PROCESSES PER SHIFT
1. Sedimentation
Manpower
1
1
1
1
Job Description
Fill tanks
Empty tank
Change hoses
Desludging
2. Filtration
3. Ion Exchange
Run influent pump
Watch columns for
loading
Backwash
Run influent pump
Watch columns for
loading
Carbon Column
2
2
Run infl uent pump
Watch columns for
loading (1 bank each)
5. Chemical Reaction
Oxidation
Reduction
Sedimentation
Neutralization
1-2
1
1
1
1
1
1
7-8
Chemical feed
Mixer
Run influent pump
Run effluent pump
Run flocculating unit
Test endpoint
Desludge (opt.)
198
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5.4.2.6 Miscellaneous Problems - Other problems can also affect the
flow rate. If the containment Is not complete, the total overflow from
the spill must be treated or held for treatment. Another consideration
is the availability of hauling vehicles for sludge removal and the
availability of the disposal site. If the proposed sludge volume per
day Is too voluminous, the flow rate must be reduced.
5..**.3 Parallel/Batch System Use
The use of the parallel batch operation does add flexibility to the
system. If the scale-up of the process changes from that which is ex-
pected or if maintenance problems occur, the addition of tanks In parallel
can compensate for these problems. The systems are set up in banks of
tanks and filters served by pumps fitted with flow splitters and then
equalization tanks between processes. If more capacity Is needed, more
tanks can be added to the operation without changing much of the basic
design criteria. The examples which follow indicate how these systems
can be modified with various limiting factors.
5..fr.4 System Flow Scheme Construction
5.4.4.1 General - Once the flow scheme has been chosen, there are some
construction steps which are not apparent from the original schematic.
Additional tanks for equalization between processes and specific process
logistics are necessary for efficient operation of a treatment system.
Therefore various procedures have been recommended and are discussed in
the following sections.
51A._k.2 Equalization Tanks - Addition of equalization tanks between
processes will stmp1i fy the operation of a batch and continuous flow
integrated system. It also provides a safety factor and extra storage
in a malfunctioning process. These tanks are not necessarily large,
but they should hold a sufficient amount of liquid between the units
to smooth out the flow rates. In general, an equalization tank Is
placed before and after each unit process. For column operation, the
calibrated equalization tanks can be used to regulate the loading rates.
5.4.4.3 Carbon Column Series Operation - Design of efficient carbon
column operation is establIshed by two criteria of equal importance.
One criteria is the loading rate to a column and this variable is a
function of the surface area of the column Itself. The other variable
is the contact time between the carbon and the contaminated liquid and
this factor is a function of the depth of carbon In the column and the
loading rate. It is necessary to provide a minimum contact time of
thirty minutes for removal of contaminants, however, the loading rate of
8l.J*l/min/sq. m or (2gpm/ft2) will only allow a fifteen minute contact time
the carbon depth is limited to I.22m (k&") (See Section 6.3.2.) Therefore,
199
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to increase the contact time a second column can be used in series with
the first column and this can be visualized as a tall column split inte
two shorter columns for easier operation. However, the surface area of
the second column is not to be considered fn the calculation of the re-
quired surface area. Another way to increase the contact time is to
Decrease the loading rate to *»Q.717min/r/f however, use of series operation
at 8l.J»l/min/sq. m or Ugpm/ft^) has several advantages. These are:
1) additional contact time to 60 minutes can be obtained by reducing the
loading rate if necessary and more importantly, 2) the exhaustion of carbon
can be monitored at the effluent from the first column to establish the actua.
breakthrough time and still provide removal through the second column.
A schematic of the carbon column operation as recommended is shown in
Figure 40.
A
A person
Q. PumP
A
carbon column
equalization
tank
Figure 40. Schematic of carbon column operation.
In this operation, however, there are requirements for additional man-
power, number of pumps and equalization tanks.
5.4. 4_. A Pump Requ I rements - Transfer of the contaminated liquid from the
water body to the treatment system, through the process and then back to
the environment Is done using pumps. Specific details on pump choices are
given In Chapter 7', Figure 41, however, the number of pumps needed and the
required capacity are established in this system design section. Using
pumps in a batch system requires a single pump which is operated at a
flow equal to or higher (if possible) than the system's design flow rate.
Tanks are filled, then hoses are switched to another tank to keep the
operation as continuous as possible, therefore, one influent and one
effluent pump are used for any number of tanks. Column operations are also
fed by one pump which operates at the system's design flow rate, however,
a flow splitting device Is used to divide the flow and allow correct load-
Ing rates. Miscellaneous pumps necessary include Individual chemical feed
pump for each chemical added, mixing pumps, desludglng or solids handling
pumps, and a final pump to return the effluent to the water body. The
pump requirements and schematics are shown in Figure 41.
5.4.5 Examples of System Design
200
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l-o
O
Process
Sedi men tat ion
Fi11rat ion
Ion Exchange
Carbon Column
Chemi cal
Reaction
Holding Tank
No. P ump s
1 - Influent
1 - Effluent
1 - Sol ids Handling
1-2 - Opt. Chem. Feed
Influent
Backwash
1 - Influent
2 - Influent
1-2 - Chemical Feed
1 - Influent
1 - Effluent
I - Mixer
1 - Des1udge
1 - Effluent
Approximate Configuration
desludge
infl.
effl
chem feed
Figure J»1. Pump requirements for unit processes.
-------
5.^.5.1 General - The following examples show a general approach to
system design. After bench scale tests have been performed on the con-
taminated liquid, and a flow scheme chosen, a detailed schematic is
developed. A summary of the equipment requirements for the various unit
processes is shown in Figure k2. The user must keep in mind these re-
quirements and the information presented in Section 5-^ when developing
the preliminary schematic.
Once the schematic is established, then calculations are begun to
establish the design flow rate. An initial approach is to choose an
approximate time which is to be considered limiting (if one does not
already exist) to provide a starting point for calculations. Once
the design has been completed at that flow rate, then the various
limiting factors should be considered. These were discussed in Section
5. *».2 and are presented in Figure 4 3 as questions to be considered by
the user after a design has been completed. Answering these questions
will force the OSC to evaluate the entire system prior to construction
and allow a decision to be made as to whether the initial design flow
rate can be attained or not. This procedure is outlined in the examples
whi ch fol low.
5 . *< . 5 . 2 Examp I e : Endr in Sp 1 11 -
Note: AH calculations are in English units, the following conversions are
appropriate.
Ibs x O.^ - kg
ft x 0.305 = m
gal. x 3.785/1000 = cum
ft2 x 0.093 - m2
gpm x 3.785 » Ipm
SECTION
REFERENCE
Scene: A train car has derailed and spilled ten kS gallon
drums of Endrin into a pond. The spill has been contained
within the pond, however a long range weather forecast indi-
cates storms are expected in 7 - 10 days. It has been
decided to treat the water column and dredge the bottom
separately but the local suppliers have only six 5' diameter
tanks available for use in treatment construction. Calcu-
late the design flow rate and system logistics to treat the
water column.
I. Choose Appropriate Flow Scheme Table 22
Carbon 100-300 #/#
202
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Gravity Separation
Column Operation
(Filtration, carbon, adsorption
'on exchange)
1. Tanks - equalization, process,
chemical storage
2. Desludging/Skimming Equipment
3. Chemical Feed System (opt.)
*t. Mixing Equipment (opt.)
5. Flocculation Device (opt.)
6. Chemicals (opt.)
7. Pumps - raw flow pumps,
solids handling
8. Sludge or Scum Tanks
9. Sampling Equipment
2.
3.
4.
5.
6.
7.
8.
Tanks - equalization, process
Pumps - influent, solids handling
Flow Spli tter
Media
Sampling Equipment
Fines Skimming Device
Underdrain system - bricks,
grating, gravel, sand
Equalization Tank (after)
General
Chemical Treatment
Precipi tation
1. Tanks - equalization, process, 1. Desludglng System
chemical feed
2. Chemical Feed System
3. Pumps - solids, raw flow,
chemical feed
4. Mixing System
5. Flocculation System (opt.)
6. Chemicals
7. Chemical Testing Kit
Neutrali zation
1. pH Meter
2. pH Meter
3. Sludge Tanks
Oxidation/Reduction
1. ORP Meter (if possible)
2. Chlorine Testing Kit (opt.)
3. Spot Plate Chemicals (opt.)
Figure ^2. Equipment requirements by process element.
203
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1, Is time limiting?
a. Is there an immediate danger or limiting period of time
before a hazard exists?
b. Do meteorological conditions impose a time limit?
c. Do local political situations impose a time limit?
d. Do other circumstances impose a time limit?
2. Is the site limiting?
a. Can the treatment site be located close enough for pumping?
b. Is the site accessible by truck?
c. Is sufficient clear area available?
d. Is sufficient flat area available?
e. Is the ground firm enough to hold the treatment system?
f. Are too many set ups needed?
g. Is the site close to residences which impose various other
restrictions?
h. Does the site impede vehicular traffic?
3. Materials avai1able?
a. Is sufficient tankage available (volume, number, type)?
b. Can pump transfer capability be obtained?
c. Is column media available?
d. Are chemicals available?
e. Is special equipment necessary and available?
4. P rocess Res triet i ons ?
a. Is an extra long time needed in sedimentation?
b. Is the sludge difficult to remove?
c. Are longer contact times required in the columns
(especially carbon)?
d. Are large volumes of sludge generated?
5. Is manpower limiting?
a. Is there sufficient skilled labor for construction?
b. Is there sufficient labor for operation?
6, Are other problems apparent?
a. Is the degree of containment sufficient to allow a chosen
flow rate?
b. Is there sufficient hauling capacity available for sludge?
Figure ^3. Questions to establish limiting factors.
204
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SECTION
REFERENCE
II. Do Bench Scale Tests
Only settling tests were performed on the water
column which contained algae with entrained endrln.
This material must be removed prior to carbon column
adsorption since It exerts a large carbon demand.
The results are as follows:
Flocculation time = 5 min.
Settling rate = 0.5 fpm
Sludge volume = 1.3% of influent flow
Sludge height = 0.5 cm.
Cylinder height = 36.5 cm.
Polyelectrolyte dose = 2.0 mg/1
III. Develop an Appropriate Schematic
I. Establish number of pumps
Explanation: Each process (or bank of tanks)
requires an influent pump. Since carbon
adsorption is done in series, it requires
two influent pumps. An effluent pump is
used after the final holding tank.
2. Place equalization tanks, denoted E , between
the unit processes
Explanation: These additional tanks will
simplify the operation.
3. Use dashed lines to indicate possible process
tanks.
k. Place a holding tank at end of the system for
effluent storage
5. Draw diagram:
O Sludge
a
Chemical Treatment
i ©© a
Figure
205
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IV. Calculate Desirable Flow Rate. -,.,.,.,«.,
SECTION
Assumptions: a. 7 day time limit REFERENCE
b. 1,000,000 gal. to treat
Flow rate = Vspi11
time to treat
= 1,000,000 ga1.
7 day "x 16 ~h r/day x 60 min/hr
= 1^8.8 gpm ^ 150 gpm
Explanation: Assume a design day of 16 hours
for treatment although actual operation may be
longer to treat backwash. Experience has
indicated that a jury-rigged system will
require large amounts of maintenance and
that backwash ing and desludging is more
easily accomplished during down time.
V. Establish Number of Sedimentation Tanks Required 6.5.4
1. Apply data from settling test to establish deten-
tion time
det. time = p r o ce ss he^ight x 3 (safety factor)
settling rate
assumption: Hp = 3 feet
settling rate = 0.5 fpm
det time = 3 ft. x 3
0.5 fpm
= 18 min:
flocculation time =• 5 min.
total detention time = 23 min.
2. Calculate fill and draw time
Assumption: Pumping rate into and out of tank
150 gpm
tank type - 20 ft. diameter pool
effective diameter = 19 ft.
process height = 3 ft.
206
-------
2
Tank volume, Vn = HP x Hp x 7.48 gal SECTION
~
REFERENCE
= 3.14 x (19)2 ft2 x 3 ft x 7.48 gal
. - -
Vn = 6360 gal.
t,., , t , Vn 6360 ,0 c •
fill = draw = -5— = TF7T" = ^2-5 nun.
Pumprate 150
T = total time = 23 min + 2 (42.5) = 108 min.
Explanation : Although a filling and drawing
rate of 150 gpm is necessary when working
through the design steps, it is recommended
that higher rate pumps actually be used for
shorter durations, allowing time in between
batches to move hoses, pumps, do maintenance,
etc.
3. Establish frequency of desludging
0.25 x Hp x TT
time between desludging
accumulation of sludge
batch
accumu 1 a t i on of s 1 udge = 0.5 cm x 3 ft. = .014 x 3 ft.
batch 36.5 cm
= 0.041 ft.
time between desludging = 0.25 x 3 ff- x 108 min.
.041 ft x 60 m in/hour
= 33 hours
However desludging can be performed after the 16
hour operating period (i.e. during the 8 hour down
t i me ) .
Calculate reduction in tank volume caused by
sludge accumulation.
Amount of sludge accumulated = amount of s hjdjje_ x
between desludgings batch
ba t che s _
before desludging
207
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amt. of = 0.041 ft x 16 hr/between x 60 min/hour SECTION
sludge batch des judging _ _ REFERENCE
accumulated 108 min/batch
= 0.37 ft. /between* des Judging r^ 0.4 ft.
Effective process heights =
Hp - amount of sludge accumulated between de-
si udgings
= 3 ft - 0.4 ft = 2.6
and the corrected tank volume (VDeff) is therefore:
(19) ''ft2 x 3.14 x 2.6 ft x 7.^8 gal
-
Vff) =5500 gal.
Explanation: This height is then equal to the actual
effective process height after reducing for accumulated
sludge over the time period. The total sludge will not
accumulate to this height until the end of the day so
the average is 0.5 times the total accumulation. How-
ever drawoff can only be done to a level approximately
twice as high as the sludge layer. Therefore the
effective reduction is the following:
2 x (0.5 x height of sludge for drawoff) = height of
s ludge.
5. Calculate process volume required
VP - Qp (Tt)
Vp = 150 gpm x 180 minutes = 16,200 gal.
6. Calculate number of tanks needed
n = Vp/Ve
= 16200 gal .
5500 gal /tank
~ 3 tanks
VI. Calculate the Number of Filters Needed, 6.2.2
o
loading rate = 4 gpm/ft
diameter of f\ 1 te.r = 5 '
208
-------
I. Calculate surface area of I filter SECTION
no2 REFERENCE
surface area = — r—
• 3.1*> x (5) 2ft2
= 19.6 ft2/filter
2. Calculate surface area needed based on flow rate
surface area = i-^ /f.2
<4gpm/ft
2
Surface area = 150 gpm = 37.5 ft
k gpm/ft
3. Calculate the number of filters needed
number of filters = surface area
surface area/filter
= 37.5 ft2
19.6 ft /filter
= 1.9
= 2 filters
VII. Calculate the Number of Carbon Columns Needed 6.3.2
o
Assumptions: diameter = 5' surface area = 19.6 ft
2
surface loading = 2 gpm/ft
a. calculate surface area needed: Qp _
2gpm/ft
150 gpm 2= 75 ft2
2 gpm/ft
b. calculate the number of columns
75 ft2 = 3.8
19.6 ft2 /column
= k columns
c. Total number = 2 x k columns = 8 columns
209
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Explanation: Carbon columns are used in series
to provide the required contact time so the SECTION
second column is not included in the surface area REFERENCE
calculation.
VIM. Design the Holding Tank
Assumptions: Hold about 30 min. flow, pump into and
from tank at 150 gpm.
Use 20' diameter tank
Use 19' feet effective diameter
Hp = 3 ft
Volume = (19) 2ft2 x l>.\k x 3 ft x 7.^3 gal
n k ft 3
= 6360 gal.
V ^
Time to fill and draw =
pumping rate/
= 6,360 gal . x 2
150 gpm
= 85 minutes
TT = 85 * 30 - 115 minutes
Vp = 115 minutes x 150 gpm
= 17,250 gai.
17,250
Number of tanks = \/p_ =~S,JGG =2.7
Vn
Use 3 tanks
Explanation: If possible the OSC should deter-
mine if 2 tanks and a shorter holding time is
suf f icient.
IX. Design Sludge Holding Tank 6.5.4.
Calculate sludge volume for one day of operation.
Assume the volume to be stored is twice the actual
volume of sludge produced since it is recommended
that drawdown only go down to twice the actual
sludge depth.
depth of sludge for storage = 2 x 0.40 ft. = 0.3 ft.
210
-------
volume of sludge for storage from 3 sedimentation
tanks = (19) ft x 0.3 ft x 3.1*> x 7.^8 gal, x 3 tanks
_ __
SECTION
REFERENCE
= 5087 gal. required
one 20' diamter tank holds 6360 gal. so 1 tank is
sufficient
X.
150
gpm*
a
Revise the Schematic:
150 ©
gpm* © (f
a ©
150
gpm
®
(A}
150
gpm-
a
(A)
(A)
150
gpm*
20'
5'
'5'
These pumps can actually be of any capacity greater than 150
gpm; the greater the capacity the shorter the duration
of their operation.
XI. Evaluate the Limiting Questions
1. Time limits - No problem since the flow rate was
established based on this criteria.
2. Site considerations
a. Safe proximity?
Answer: Yes, it Is safe to approach and treat.
b. Accessible by tru:k?
Answer; Yes.
c. Is area clear/flat/firm and available?
Answer; The amount of area required can be
estimated be assuming 5' between large tanks
and 21 between small tanks and then adding
the distances from the schematic. In this
case an area 105 ft. x 85 ft is needed and
Is avallable.
d. Are residences or roads near by which would
restrict operation or operating hours?
Answer: No.
e. How often must the treatment system be set up
and can the site be centrally located:
Answer; The site can be centrally located
and set up only once.
Figure
211
-------
3. Material availability
SECTION
a. Are enough tanks available? REFERENCE
number needed number available
1-25' diameter
20' 9 (sedimentation/sludge/ 0
1 equalization/holding
tank)
5' 10 (columns) 6
10' 3 (2 equalization/carbon 2
storage) 1-18' diameter
b. Are sufficent numbers of pumps available? 7.2
see references Available
Number Rates to be pumpec[ number pump size
3 ^150 gpm 3 - ^00 gpm
3 - 150 gpm 3-150 gpm
1 - 25 gpm backwash 1 - 50 gpm
1 50 gpm solids pump 1-100 gpm
c. Is media available? 6.3.2
Amount needed = 100-300 #/# of soluble
material.
Solubility of endrin = 0.19 mgA in water
Volume of spill = 1,000,000 gal.
Ibs of Endrin = volume (MG) x 8.3A Ib x solubility
in mg/£. MG-mg/1
= I MG x 8.31* Ib x 0.19 mg/1
MG-mg/1
= 1.58 Ibs of Endrin is soluble,
the remainder is entrained or
sunk.
Amount of carbon to order =
1.58# x 300#/# of soluble Endrin « 1»75 Ibs.
Answer: Yes. Carbon is available.
d. Are chemicals for flocculation available?
Amount of chemicals needed;
212
-------
SECTION
REFERENCE
polymer added; 2.0 moA x 3*784 1,/gal. x 10 gal.
~~" 453.6 gr/# x 2000 mg/gr
Jbs of polymer = 17 Ibs needed
Answer; Yes. Chemicals are available.
e. Does spill require special equipment?
Answer: No.
k. Process restrictions
a. Is the detention time too long?
Answer: A 23 mln. detention time is not too long.
b. Are problems involved with desJudging?
Answer; No apparent problems for water column treatment.
c. Long contact time needed in column?
Answer; No. Endrin will adsorb well.
d. Are large volumes of sludge obtained?
Answer; No. Only 1.3% of influent volume is
estimated to become sludge.
5. Manpower limitations
a. Construction: 10 people are available -
enough people.
b. Operation: See Table 2k. The number of people
needed per shift of operation is as follows:
sedimentation - 3 carbon - k
filters - 2 effluent pump - 1
Add 3 people for safety, process and maintenance
directors.
13/shift and 2 shifts/day for operation
c. Downtime crew
This crew should equal the number of people on the
operating crew during one shift. In this case 10
people.
d. Total manpower In operation « 26 + 10 = 36 people
213
-------
SECTION
6. Miscellaneous REFERENCE
a. Is the spill sufficiently contained to be
stable for 7~10 days?
Answer: Yes.
b. Is their sufficient hauling capacity for
5050 gal. of sludge/day?
Answer: Yes.
Evaluation indicates that the sufficient tankage
is not avaialble to handle the flow rate. The
system must be modified.
XII. Draw an Appropriate Schematic Utilizing the Available
Tanks.
Criteria - tanks - 6-5' diameter tanks
A-181 diameter tanks
1-25' diameter tank
2-10' diameter tanks
An 18 foot tank has an effective diameter of 17-5 feet,
pumpage ^ the same
(T) carbon
Establish flow through each unit process:
choose the smallest as limiting process flow.
a. sedimentation: volume available
TT
T = fill & draw time + settling time
Vn = (17.5) 2ft2 x 3.H x 7.A8 gal, x 3 ft.
539^.7 gal.
7_gal =36min.
gpm
2-1 k
-------
TT - 2(36 min) + 23 min.
= 95 min.
Volume available = 2 x V
n
gpm = 2(5394.7) gal
95 min.
= 114 gpm
b. Number of columns (same as filter & carbon).
2 2
for filters: surface area = 3.14 x 5 ft
SECTION
REFERENCE
= 19.6 ft*
2
design = 4gpm/ft
flow - 4gpm X 19.6 ft2
ft2
= 78.5 gpm
Therefore the operating flow must not exceed
78.5 gpm.
(S) 78.5 _ 150 gpm 3 >_ 78.5 gpm
3 - 150 gpm 3 - 78.5 gpm
1 - 25 gpm 1 - 25 gpm
1 - 50 gpm 1 - 50 gpm
«
All other elements are the same.
215
-------
The responsibility Is now up to the OSC to determine if the time SECTION
factor is more critical to the cleanup operation than the tank REFERENCE
shortage. If so, tanks must be made available from any source.
If not, the OSC can use available tankage for construction.
5 . 4.5.3 Examp 1 e : Sod i urn Cyan i de Spill -
Note: All calculations are in English units, the following con-
versions are appropriate:
Jb x 0.454 - kg
ft x 0.305 = m
gal . x 3-785 x 10 = cum
2 2
ft x 0.093 = m
gpm x 3«784 = 1pm
Scene: A truck carrying five 200 Ib. drums of 30% sodium
cyanide has spilled into a slowly flowing river. A dam has
been placed downstream and the upstream water is diverted
around the contaminated portion of the stream. Approxi-
mately 1,900,000 gallons of water has been contaminated and
the bottom of the stream is also affected. It has been
decided to dredge the top layer of the bottom and treat the
river water in one operation. A presettler and sedimentation
are necessary. It is desired to treat the entire spill with-
in 5 days, however only an area 105' x 75' is available for
treatment. Establish the most feasible flow system for this
si tuation.
I. Choose Appropriate Flow Scheme Table 22
NaOH, + HOC1 HCl Add Na(OH) to pH 8.5 then add
HOCl/10% excess/react 1 hour/
neutralize to pH 7 if needed.
II, Do Bench Scale Tests
a. Settling tests: settling tests were done and it was
found a presettler was needed. Polyelectrolyte was
added at 5 mg/1 with a flocculation time of 5 minutes
The settling rate was 0.4 fpm.
b. Oxidation tests indicated that 5 ml of IN NaOH were
needed to raise the pH to 8.5 and 10 ml of 0.05£
216
-------
hypochlorite solution were added per liter of sample.
The mixture reacted one hour to degrade cyanide to
cyanate and carbon dioxide and nitrogen.
c. Neutralization required only 2 ml of IN HCl to return
the pH to 7-
d. Since no sludge was formed it was established the
oxidation and neutralization could occur in the
same tank.
SECTION
REFERENCE
III.
e. Sludge volume from the presettler was approx-
imately k% of the wastewater influent and the
height of sludge after sedimentation was 2.0%
of the total height.
f. Summary of bench test results.
1) presettling - k% volume of wastewater is
sludge.
2) sedimentation - polyelectrolyte dose -
5 mg/ £
settling rate - O.^fpm
sludge volume - 2.0%
5 minute flocculation time
3) chemical treatment - NaOH - 5ml
HOC1 - 10 ml of
HCl - 2ml
Develop an Appropriate Schematic.
(si
Figure
Q
IV. Calculate Desirable Flow Rate.
V
spill
Time to treat
1.9 x 10 gal.
5 day x 16 hr x 6d~mln
day hr
400 gpm
Exp1 anatIon: Assume 16 hour per day operation. Use
other 8 hours for maintenance, desludging, chemical
mixing, etc.
V. Calculate Number of Sedimentation Tanks Required.
6.5.4
217
-------
1. Apply data from settling tests to estimate deten- SECTION
tion time. REFERENCE
detention time = process height x 3(safety factor)
settling rate
parameters: settling rate = 0.4fpm . 6,5,**
process height, Hp = 3 feet
flocculation time = 5 min.
detention time =3 ft. x 3 = 22.5 min.
0.4fpm
Total detention time = 22.5 min + 5 min. = 27-5 min.
2. Calculate fill and draw time.
Assumption: Pumping rate = 400 gpm (in 6 out)
tank type = 25' diameter
2k1 effective dia.
7 3' process height
tank volume = V = HP Hp x 7.48 gal.
n 4~ ft 2
" (3.1*0 x (24)2ft2 x 3 ft x 7.^8 gal.
Z» ff3
= 10,146 gal.
Tflll = Tdraw = n « 10,146 gal. = 25.4 min.
pump rate 400 gpm
TT = total time = 2(25.4) min. + 23 min. = JB.B min.
=« 79 min.
3. Establish frequency of desludgJng.
Time between desludging = 0.25 x Hp x T
accumulation of sludge
batch
Accumulation of sludge = 0.02 x 3 ft = 0.06 ft
batch batch
Time between desludging = 0.25 x 3 ft x 79 min. =
0.06 ft/batch
= 988 min.
= 16.5 hours
218
-------
Therefore desludging can occur after operation 16.5 SECTION
hours. REFERENCE
Calculate reduction in tank volume caused by
sludge accumulation.
Amount of sludge accumulated = amount of sludge x
between desladings batch
batches
before desludging
Amount of sludge accumulated *
0.06 _ ft x 16 hr/between desludging x 60 min./hour
batch 79 mIn./batch
- 0.73 ft between desludging
Effective process height = Hp - height of sludge
accumulated between desludgings.
3 ft - 0.73 ft - Hp (eff) - 2.27 ft
Vn (eff) = (2M2ft2x3.1^ x 2.27 x 7.^3 gal.
k ft3
Vn(eff) - 7.677 gal.
5. Calculate process volume required
Vp = 0_p (TT)
= *fOO gpm (79)xminutes
= 31600 gal.
6. Calculate the number of tanks needed
Vp = 31600 gal. = h.\ tanks
V ff 7677 gal/tank
nerr r .
= 5 tanks
VI. Calculate the Number of Oxidation/Neutralization Tanks.
1. Calculate fill and draw time.
Assumptions: pump capacity - ^00 gpm
tank diameter- 25'
effective tank diameter - 2V
219
-------
process height - 3' SECTION
tank volume - 10146 gal. REFERENCE
2. Fill time = draw time - Vn = 10146 gal = 25.4 minutes
pump capacity 400 gpm
3. Calculate total detention time
T = (25.4 min)x2+ 60 min for total reaction =
110.8 min.
= 111 min.
Explanation: Reaction time is very short for
neutralization so the oxidation is the most time
consuming.
4. Establish tank volume needed
Vp = Qp (TT)
= 400 gpm x 111 min.
= 44,400 gal.
5. Calculate number of tanks needed
N = Vp
Vn
= 44,400
10146
= 4.4 tanks
= 5 tanks
Explanation: No sludge accumulates in this process
so entire volume is available.
VII. Calculate Number of Sludge Tanks 654
Volume of s1udge = Vp x 0.04 x hour of operation
day day
* 400 gpm x 0.04 gat, sludge x 16 hr/day x
gal. influent
60 m!n./hr.
- 15,360 gal./day
220
-------
Assumptions : 25' diameter tank SECTION
3' process height REFERENCE
Vn = 101*»6 gal. "
Number of tanks - volume sludge/day jc - ^
v°lume/ta"nk = i c * 1A6
=1.5 tanks
» 2 tanks
Explanation: Sludge is removed once per day.
VIM. Estimate Number of Presettling and Equalization Tanks.
1 - presettler - 3000 gal tank is good
1 - equalization - 25' pool, 3' Hp
IX. Calculate Number of Holding Tanks Needed.
Assumption: holding 15 min. of flow
pump into tanks at - *»00 gpm
tank volume - 101A6 gal.
T = Total time = 2 (101A6 gal) + 15 min. = 65-7 min.
¥00 gpm
fill & draw time
Vp - Qp x TT
= **00 gpm x 65.7 min.
- 26280 gal.
n = Vp » 26280 gal = 2.6 gal ./tank
"W 101A6
n = 3 tanks
X. Revise the Schematic
25'
221
-------
XI. Evaluate the System.
The 1st limiting factor to consider is the space
requirement: The system @ 400 gpm requires 115' x
140' and only 105 x 70' is available.
Therefore more consideration is necessary.
XII. Modify the system to comply to limiting factors of the
Space Requirement.
SECTION
REFERENCE
Figure 43
Trial
Establish available tanks.
3 types are available
D (feet) calculation
18'
20'
25
(17) 2ft2 x 3-14 x 3 ft 7.48/4
(19) 2ft2 x 3.14 x 3 ft 7.48/4
(24) 2ft2 x 3.14 x 3 x 7.48/4
Volume (gal)
5090
6360
10146
2.
See how many tanks fit one area approximately
60 x 100 (accounting for spaces between the tanks).
222
-------
Trial ] 20' D tanks - 11 tanks or 69960 gal.
Trial 2 25' D tanks - 6 tanks + 2 20' D - 60876 + 12720 - 73596 gal
Trfal 3 18' D tanks - 15 tanks or 76350 gal.
Trial 2
Trial 3
223
-------
The usage of tanks could then be calculated based on the following
system. SECTION
REFERENCE
3. Estimate the best allocation of tanks to processes.
4. Develop a new flow rate based on a comparison of
the two tank total volumes:
System 1 - 17 25' 0 or 10,146 gal. tanks - 172,482
System 2-15 18' D or 5,090 gal. tanks = 76,350
Assume that 5 of the tanks will be used for the 0/N
step and 4 for sedimentation.
5. Calculate the fill and draw times.
In this case we already know the number of tanks
available,therefore it is necessary to first cal-
culate the effective tank volume taking into con-
sideration the accumulated sludge as follows:
(17) 2ft2 x 3.14 x 2.27 ft x 7.48 gal = 3852 gal.
j.—j-
Since the process flow rate is unknown, the fill
and draw times are as follows:
TT sedimentation = 28 min + 2 (3852 gal)
Qp
TT 0/N » 60 min + 2 (5090 gap
Qp
6. Knowing the allowable process volumes, solve for
the process flow rate, Qp using:
Vp - °-P * TT
For sedimentation:
V = 4(3852 gal) = Qp x (28 min + 2 3852 gal )
P ~QP~
=15,408 = Qp(28) + 7704
7704 = 28 Qp
275 = QP
Qp = 275 gpm
224
-------
For 0/N:
Vp - 5 (5090 gal.) =- Qp x (60 min + 2x5090 gal.)
QP
= 25^50 = Qp x 60 + 10180
15270 = 60 Qp
25** - Qp
Qp = 25** gpm
Therefore the design processes flow rate Is the
lower of the two, or 25*» gpm.
7. The resulting tank utilization would then be:
Number Type
1 presettler
2 sludge tank
A sedimentation tank
1 equilization tank
5 oxidation reduction tank
2 holding tanks
XIII. Compare the Two Systems.
Now evaluations of the limiting factors is necessary
for both situations.
Time 1imi ts:
Site 1imits:
Materials:
location close
access i ble
clean area
flat area
f i rm area
setups
res idences
vehicular traffic
tanks
pumps
Initial
Design
5 days
Alternate
Design
8 days
yes yes
yes yes
no; need 115' yes; 105'
x 1^0'
no
yes
OK
no
no
x 70'
yes
yes
OK
no
no
17-25' D yes
15-18' D; yes
1-20 gpm (solids) yes; same
2-10 gpm chem feed
225
-------
Process Restric-
tions:
Manpower Limits:
Miscellaneous:
media
chemicals
spec, equipment
settling rate
desJudging
contact time
sludge volume
construction
operation
contaminant
hauling capacity
not needed
yes
not needed
no problem
no problem
N/A
same
no
no
no problem
OK
not needed
yes
not needed
no problem
no problem
N/A
same
no
no
no problem
OK
The choice Is then left to the OSC to establish If the time restric-
tion Is more critical than the space problem. Possibly more flat
area could be cleared for use but the expense and possible time lost
may negate the benefits. Each situation must then be evaluated on
its own merits.
SECTION
.**.5.*< Example; Ammonium Persulfate Spill - REFERENCE
Note: All calculations are In English units, the following conversions are
appropriate:
Jb x Q^ m kg
ft x 0.305 = m
gal. x 3.785 x 10 = cum
ft2 x 0.093 - m2
gpm x 3.78*» = 1pm
Scene: A truck carrying six 50 pound packages of ammonium persulfate
has spilled into a swamp. The spill is contained but needs treatment
within 3 days. The total spill volume Is 500,000 gallons of sllty swamp
water which requires long periods of clarification. However, a limited
number of swimming pools and area are available for use. Therefore the
OSC must evaluate the situation and choose the best alternative.
I. Choose Appropriate Flow Scheme
Na BisulHte
Add H2SOi,to pH 3/add bisulfite to large ORP
change or indicator change/neutralize to
pH 7 with NaOH/fIIter/exchange/neutralIze
to pH 7 with NaOH
Table 22
226
-------
II. Do Bench Scale Tests
1. Settling tests: A polymer was added In dosages
of 25 mg/1 and the material was allowed to
settle. The settling rate was 0.1 fpm. Floccu-
lation required was 10 min. Sludge accumula-
tion was I.1 cm.
2. Reduction and neutralization test: 15 ml of
IN H SO. was added per liter of sample to
reacfi pH of 2 with addition of 10 ml of
100 mg/1 sodium bisulfite to the indicator
change. (Needs 10 min for reaction.) An
additional 10 ml of IN NaOH returned to pH 7
3. Extra NaOH was ordered to allow readjustment
of the pH after ion exchange.
4. Cation analyses were performed to establish
need for ion exchange media.
III. Draw an Appropriate Schematic
SECTION
REFERENCE
6.5.2
6.6.7
Figure 41
chemical
feed
The initial neutralization can be done after
reduction is complete in the same tank and
the final neutralization can be done in the
holding tank.
IV. Calculate Desirable Flow Rate
Assumption: 3 days to clean 500,000 gal. spill
500,000 gal.
flow rate
3 day x 16 hr/day x 60 hr/min ~ 175 gpm
Explanation; Use 16 hr/day operation to allow time
for maintenance of the system.
V. Establish Number of Sedimentation Tanks Required
1. Apply data from settling test to establish
detention time:
6.5.4
227
-------
SECTION
REFERENCE
detention time = X 3 (safety factor)
Assumption: Hp » 3
settlIng rate = 0.1 fpm
Detention time, tj = 3 ^.x 3 = 90 mln
Flocculatlon time « 10 min
Total detention time » 90 mln + 10 mln * 100 min.
2. Calculate fill and draw time
Assumption; pumping rate Into tank: 175 gpm
tank - 25' dta.
2V effective diameter
3' process height
T i , u 3.14 x (2k)2 ft2 x 3 ft x 7.^8 gal
Tank volume Vn « i—• jr-= Ft3' —
= 10,146
V
fill time - draw time
pumping rate
gpm
Total time (TT)-2(58.3) min + 100 min = 216.6 min.
3. Establish Frequency of Desludging
Time between desludging - - • — S> ^ T -. — rr - r- x TT
3 y accumulation of sludge/batch '
Process height = 3 feet
accumulation of sludge , Klcn^ t
oaten .jo.o cm
Time between desludging - °'25 x 3 6'6 mln
228
-------
SECTION
REFERENCE
- 1,805 mln
=* 30.0 hours/between des Judging
However, the desludgfng can be performed after the 16
hours operating period.
Calculate reduction In tank volume caused by sludge
accumulation
amount of sludge accumulated between desludgfng =•
amt of sludge _ batches
batch X before desludging
'. x 16 hours/desludge x 60 min/hr
Datcn 216.6 min/batch
• 0.398
approx. 0.^ ft
5. Calculate effective process volume
Hp - height of sludge accumulated * effective process height
between desludging
3 ft- O.A ft = 2.6 ft
Volume tank - (3.1*0 (2k)2 ft2 x 2.6/ft x 7. ^8 gal.
= 8,793-6 gal.
6. Calculate process volume required
V - % 'V
= 174 gpm (216.6 min)
- 37,689 gal.
229
-------
SECTION
REFERENCE
7. Calculate number of tanks needed
n- J&
• 37.689 gal.
879^ gal/tank
= 4.3 tanks
n « 5 tanks
VI. Calculate number of chemical reaction tanks 6.6.9
1. Apply data from bench tests to establish a detention time.
a. Neutralization - 10 minutes
b. Reduction - 15 minutes
c. Safety factor - 5 minutes
30 minutes
2. Calculate fill and draw rates
Assumption; \Tk gpm influent rate
Tank specs: 20' diam.
19' diam.
3' process height
6366 gal. process volume
fill and draw time = — ffi6 galt =• 36.6 min.
pump rate 174 gpm J
TT = (36.6) 2 min + 30 = 103.2 min.
3. Is desludging necessary? No
Explanat ion: The tank is mixed continuously and no sludge
is formed". Solids entering the process
have been removed in the sedimentation tank.
k. Calculate Required Process Volume
230
-------
SECTION
REFERENCE
V - 17A gpm (103.2) min.
- 17,957 gal.
5. Calculate Number of Reaction Tanks Needed
V
N - -E.
V
n
- 17.957 gal.
6366 gal./tank
= 2.8
= 3 tanks
VII. Calculate Number of Filters Needed 6.2.2
Assumptions; 1 7*» gpm flow rate
^
Loading rate » k gpm/ft
V diameter filters
1. Calculate Surface Area of One Filter
2
surface area = irD
3.U x (M2ft2
Zj
2
= 12.56 ft
2. Calculate Surface Area Needed Based on Flow Rate
surface area
gpmft
gpm
gpm/ft''
. 5 ft2
3. Calculate Number of Filters Needed
number of filters « surface area
surface area/filter
231
-------
.5 ft
SECTION
REFERENCE
2
12.56 ft2/filter
= 3.46 filters
= k filters
VIM. Calculate Number of Ion Exchange Columns Needed 6.4.2
Assumptions: I Ik gpm flow rate
2
Loading rate - 2 gpm/ft
5' diameter columns
1. Calculate Surface Area of One Column
2
surface area = IIP
columnk
2
= 19«6 ft /column
2. Calculate Surface Area Needed Based on Flow Rate
CL
surface area needed
M gpm
2 gpm/ft2
= 8? ft2
3. Calculate Number of Columns Needed
surface area
surface area/coTumn
2 gpm/ftz
8?
-6 ft2/column
= k .k columns
= 5 columns
232
-------
IX. Design the Holding Tanks
Assumption: 1 hour's flow at 1
2V pool
2V effective diameter
3' process height
10,146 gal. process volume
gpm (60 mfn)
SECTION
REFERENCE
1. Calculate Fill and Draw Time
fill time = draw time =
= 10U6 gal .
174 gpm
flow rate
58.3 mln.
TT - 2(58.3) min + 60 min = 177 min
2. Calculate Process Volume
gpm x 177 min
30,798 gaK
3. Calculate Number of Tanks
30.798 gal.
10,11*6 gal ./tank
3 tanks
X. Design Sludge Holding Tank
Calculate sludge volume for one day of accumulation.
The volume to be stored Is calculated based on twice
6. 5.
233
-------
SECTION
REFERENCE
the sludge depth due to Ineffective draw off techniques
Volume of sludge for storage from 5 sedimentation tanks
(24)ft2 x 0.8 ft x 3.1^ x 7.^3 gal, x 5 tanks
k ft3
• 13,529 gal.
Assumption: 20' diameter tanks
19' effective diameter
3' process height
V (I9)2ft x 3.11* x 3 ft x 7.48 gal.
.3
ff
6360 gal./tank
number of tanks = s 1 udge - 13529
V ""
= 2.1 tanks
use = 2 tanks
Explanation: Store excess sludge in reaction tank after
final batch.
XI. Revise the Schematic
CD
/^\
® ((x)
gpm (D CD (D (R/N) (D
fl w
(IX) (TT)
© (IX) ® ngpm
IX) 00
-------
XII. Evaluate the System
1. Time Limit - The flow Is based on time.
2. Site considerations:
a. Safe proximity?
Answer; Yes, It Is safe to approach and treat.
b. Accessible?
Answe r; Yes.
c. Is area clear/flat/firm and available?
Answe r; The area available is not optimal to
handle 8-25' dia. pools and 5-20' diameter
pools, so a reduction in this area would be
desi rable.
d. Proximity to residence?
Answer; No.
e. Number of setups required:
An swer; 1
3. Material Availability
a. Are enough tanks available?
Answer: No.
Type
SECTION
REFERENCE
Figure *»3
No. Needed No. Available
8
5
0
3
5
k
b. Are suffi
Answer:
Number
7
1
k
2
3
3
3
5
k
clent pumps available?
Yes.
Rates to pump
>17A gpm
sol ids handl ing
5 gpm chem. feed
25'
20'
18'
diam.
diam.
diam.
10' diam.
5' diam.
V daim.
Aval 1 able pumps
8 - 250 gpm
1 " 50 gpm
k - 6 gpm chem. feed
235
-------
c. Is media ava!lable?
1) Ion exchange?
Answer: Yes.
2) Chemicals?
Answer: Yes.
3) Special equipment?
Answer; No.
A. Process restrictions?
Answer: None
5. Manpower limits?
a. Construction - 10 people available
b. Operation - 25 people available
c. Direction - 3 people available
Therefore, manpower is not critical.
6. Miscellaneous?
Answer: No 1imi ts.
XIII. Draw Appropriate Schematic Utilizing Available Tanks and
a Smaller Area
® £ (D
(D p (si) (f) f/k (D ©
t \ ^—-*^ ^~~s \^ ^/ v^_X
25' O
©
©
XIV. Calculate a New Flow Rate
The effective volume of the sedimentation tanks must be con
sidered first. The sludge accumulates to O.k ft
Veff - 8794 gal.
236
-------
Since the process flow rate Is unknown, the total times are
calculated as follows.
TT sedimentation - 100 + 2
TT R/H = 30 + 2
P
T U/t = ,0 + 2
Next the process flow rate is solved for, using the known
volume of tankage for sedimentation.
Vp = 3 (8794) - Qp (100
26,382 - 100 Q + 17,588
P
100 Q - 8,794
P
Q • 87.9 gpm
For R/N:
V = 3(6366) =Q
19,098 = 30 Q + 12,732
P
30 Q = 6366
P
Q =212 gpm
P
For H/N:
n = 3 (5090) - Q (10 + 2 5090 )
P p ^p
15,272 - 10 Q + 10,180
10 0= 5092
0. » 509 gpm
237
-------
Note: The limiting 87.9 gpm flow rate is to be evaluated by
the OSC. If it is acceptable, the following schematic results
are as predicted.
238
-------
6.0 CHAPTER 6 PROCESS CONSTRUCTION AND OPERATION
6.1 GENERAL
The following subsections detail the information needed for both the design
and construction of the various components used in the treatment scheme.
This chapter Is broken down into 5 parts: filtration, carbon adsorption,
ion exchange, gravity separation and chemical reaction. Each of these parts
Is further subdivided Into a process description, bench testing proce-
dures, design considerations, construction details, operation and mainte-
nance and troubleshooting.
It is critical that the user of the Manual be familiar with the format and
the content of this subsection. The process description is intended to
provide background information to the user and some clarification for assump-
tions used in the d*sign. Bench testing procedures are outlined for gra-
vity separation and chemical reaction treatment schemes and should be per-
formed on site or at a nearby laboratory on an actual sample of the waste-
water to be treated. It will be necessary for the user to be familiar with
the techniques and the chemicals presented, prior to actual field operation.
The same need occurs with the design and construction section. The direc-
tions are indicated as steps with indented cautions, explanations and
examples. It is intended that the steps alone can guide the user with
reference to the other columns only when necessary. However, previous
familiarity to these comments will aid the user In the field.
To use this part of the manual effectively, the user will refer to the por-
tion |ust following the process description. For column operations, this
is entitled: Design of Columns, and for chemical reaction or gravity separa-
tion: Bench Testing Procedures. The remainder of the instructions will
then follow based on the results obtained.
6.2 FILTRATION
6.2.1 Process DescrIptIon
Filtration is designed to remove particulate matter by passing contaminated
water through a layer of porous media. The applications for this treatment
vary from a pretreatment step to provide clarified water to a carbon column
or Ion exchange system to a polishing step for removal of fine partlculates
after a precipitation reaction.
Various types of media and modes of operation are used in filtration. How-
ever, a simplified mode is needed for field application and therefore a
gravity flow dual media column filter has been chosen. The effectiveness
of this type of filtration Is a function of:
a. The concentration and characteristics of the solids In suspension.
b. The characteristics of the filter media and the mode of operation
239
-------
(media sizes and depths, filtration rate, and terminal head loss).
The filter design presented in this section can provide adequate filtration
under a wide variety of solids loading conditions.
Off stream dual media filtration is operated in a column as a gravity down-
flow process. During a filter run, the process head loss will gradually
increase due to accumulation of solids within the filter media. When this
head reaches the limit set by the hydraulic conditions of the design, the
filter run must be stopped and the filter backwashed. A common fault with
filters, especially single media filters, is surface blinding which can
shorten the filter run. Dual media filters, utilizing coal above sand,
act to give better depth filtration. Backwash involves passing clean process
effluent through the filter in a reverse direction and at a rate several
times greater than forward flow rate. For downflow gravity filters, the
terminal head loss before backwash depends primarily on the available free-
board above the filter media, which is limited by the available tank height.
In addition, the effluent quality requirement may control termination of
filter runs because effluent quality decreases as the process head loss In-
creases. It is desirable In filter design that acceptable effluent quality
be produced within the entire head loss range. Acceptable1 effluent quality
may be dictated by the necessity to efficiently remove contaminated solids
from the water stream, or to provide a pretreatment for subsequent pro-
cesses which would be fouled by solids, such as carbon adsorption or Ion
exchange.
Filters are usually backwashed with stored filter effluent and backwash
wastes are usually retreated and refiltered. Therefore, the total volume
treated per filter cycle equals the forward flow volume minus the backwash
volume. Generally the higher the solids loading the shorter the filter run
and thus the lower the net process flow rate. It is usually easier in the
field to set up and operate gravity separation tanks than it is to construct
and operate filters. Filter backwash is time consuming, varying from one-
half to one hour per filter, and may be manually complicated In systems which
must be constructed without the availability of valves or separate backwash
pumping systems. In some cases, the filter pump will have to double as a
backwash pump, and switch-over from forward to reverse flow will require that
hoses be relocated. Personal safety dictates that the number of hose re-
locations be minimized. Another benefit of extended filter runs Is the
flexibility it affords in scheduling backwash during process shutdowns or
other convenient times.
The filter is a rather difficult process to construct In the field. Thus
the mode of dual media filtration outlined In the subsequent design sec-
tion was scrutinized to simplify field construction and operation as far as
is practicable.
240
-------
6.2.2 Design of Dual Media Filters (43. 44)
I. Determine the required filter area from the process flow rate using
Figure 44.
Explanation; Required filter area is based on a design filtra-
tion rate of -
,63 !42i2i (4 gpm/ft2)
m2
Operational ranges may vary from 80-240 l/m*"' (2-6 gpm/ft2)
m
Example^; (from Figure 44) At 212 l/min, a filter area of
1.31 m2 wi11 be required.
2. Select a filter tank from Section 7-3 with the following limitations;
a. A tank with vertical sides (Types A, F, G, H).
b. An above-ground tank.
c. A minimum height of 2.7 m (105 in.).
d. A diameter in the range of 0.61-1.2 m (24-60 In.).
Explanation: In tanks over 1.2 m (60 in.) in diameter,
a single outlet will probably not be suffi-
cient to permit uniform flow distribu-
tion necessary for adequate backwashing.
Multiple outlets would be required for
these filters or the construction of a
header lateral system (not covered in
these instructions).
e. A flat bottom which can be uniformly supported, e.g., lay-
ing flat on the ground.
f. Tank wall construction into which a hole may be machined for
an outlet.
3. Order filtration media using the following specification and media
volumes from Figure 44. Suppliers are listed In Section 7.9
S\ I lea Sand Anthracite Coal
Effective size (mm) 0.59-0.60 1.00-1.20
Uniformity Coefficient 1.35-1.70 1.25-1.80
241
-------
ft2 „'
m
3 ft"
21.5
16.1
1-31
m2
cc.
<.
JO.8
0
FILTER AREA
I- 1.0
-0.5
0.2 -
0.0
3-1
2.1
I.I
-I
150 200
39.6 52.8
250
66.0
<
p
s:
u.
o
LU
r>
c
L/Min. o 50 100
GPM 0 13.6 26.k
ASSUMPTIONS
I. FILTER AREAS BASED 0'! HYDRAULIC LOADING OF 163 l/min/sq m ('i gpm/sq ft)
2. 203 EXCESS MEDIA SPECIFIED TO ALLOW FOR SAFETY FACTOR AND SKIMMING.
Figure hk. Filter area and media requirements.
-------
Explanation^ The effective size range of anthracite coal
listed above is a minimum requirement. If
a lower effective size Is used, skimming of
fines will be required per Section 6.2.4.
The lower the uniformity coefficient, the
better.
Example; (from Figure 44) For the flow rate of 212 l/m'n>,
-» , m
0.5 ir of sand and 0.66 m* of coal will be required.
4. Order gravel for media underdrains from a local sand and gravel
yard using amounts from Figure 45. Order equal amounts of pea gra-
vel, and #1 and #2 gravels, and one-half that amount of torpedo sand.
Explanation; Pea gravel is about 0.31 cm (0.23 in.) in diameter;
#1 gravel ranges In size from 1.25-1.9 cm (0.5*
0.75 in.); #2 gravel ranges In size from 2.50-2.90
cm (1.0-1.5 in.).
Example; (From Figure 45) For the flow rate of 212 l/mln.,
and an underdrain area of 1.31 order the following
quantities:
Torpedo Sand - 0.75 m^,
Pea Gravel, #1 and #2 gravels - 0.55 m .
6.2.3 Construction Options for Filters
Preferred option - gravity outlet (Figure 46)
Fully gravitational flow, with a free discharge leading to an equalization
tank or a combination equalization and backwash storage tank.
Explanation;
Advantages;
Gravity discharge rather than suction from a pump is de-
sirable to prevent air blinding of the bed.
Easy to operate and monitor effluent quality. Outlet lo-
cation permits bed to remain submerged after batch runs, a
desirable feature. Can be hydrauiicalty connected with
hoses and a total of six hose fittings, eliminating the
necessity of piping and valves.
In cases where hazard to personnel would exist from contact
with fluid, piping and valves could be installed to elimi-
nate the necessity to transfer hoses when shifting from the
forward flow to backwash mode.
Two pumps may be used handling both forward flow and backwash, providing the
CAUTION:
2^3
-------
-ft
tu
§
oc
i
12.5
10.71
8.93
7.
5-36
3-57
1.79
ho.35
- 0.30
^0.25
H 0.20
- 0.15
PEA GRAVEL,
#1 AND #2 GRAVELS
- 0.10
- 0.05
m2 0
(ft2)
TORPEDO SAND
0.5 1.0 1.5
(5.38) (10.76) (16.15)
UNDERDRAIN AREA
2.0
(21.53)
ASSUMPTIONS
I. 20% EXCESS SPECIFIED FOR SAFETY FACTOR.
Figure A5- Amounts of underdrain material required for column system-is.
-------
FORWARD FLOW MODE
INFLUENT
PUMP
FILTER COLUMN
DISCHARGE
PUMP
SURGE
TANK
EQUALIZATION AND
BACKWASH STORAGE
BACKWASH
WASI£_JANK
BACKWASH MODE
TO
SEDIMENTATION
TANK
BACKWASH
WASTE
4 SUCTION
HOSE
f
BACKWASH
SUPPLY PUMP
SURGE
TANK
Figure 46. Preferred option and operating modes - filtration
-------
pump capacities are determined from backwash requirements and that they can
be throttled to accommodate forward flow and backwash flow conditions. This
option is well-suited to a parallel-flow arrangement utilizing multiple fil-
ters and a single equalization tank.
Explanation; The benefit derives from the fact that backwash flow rate
Is four times forward flow rate. Thus, in a single filter
system, both pumps operate in the forward mode at 25%
capacity. On the other hand, if two filters are used, the
same pumps could operate at 50% capacity in forward flow,
with the stipulation that the filters be backwashed In-
dividually. With three and four filters the pumps would
operate at 75% and 100% of capacity respectively In the
forward flow mode.
Any type tank may be used for equalization, in-ground or above ground, pro-
vided that the wall height be lower than the filter discharge height.
6.2.4 Construction Steps for Filters
Preferred Option - gravity outlet (Figure *»7)
'• Construct tank shell and bottom as instructed in Section 7-3.3.
2. Install brick supports for an expanded metal grating underdrain sup-
port. Note that all bricks are to be oriented radially with the
center of the filter, except the bricks on the periphery which are
oriented tangentially. For a one piece grating use about 12 bricks
per square meter.
Explanation; During backwash the distribution of water in the
underdrain area Is critical. Symmetrical, radial
orientation of bricks assists in backwash flow
distribution.
3. Install an expanded metal grating covering the complete filter area.
The maximum opening in the grating should not pass a 2.5 cm (I in.)
sphere. Standard 3.0 Ib, *».0 Ib, or 5.0 Ib expanded metal grating
will meet this requirement. Construct from one piece if possible.
If installed in multiple pieces, be sure the free edges are supported
sufficiently (almost continuous support of free edge). Fit grating
so that no gaps over 2.5 cm (I in.) In diameter exist anywhere.
A. Install the discharge line as shown, tied on one end to the grating
and extending through the tank wall at 1.27 m (50 In.) above the
base of the filter. Discharge line size is given In Table 25.
5. Install the three layers of gravel and 33 cm (13 in.) of filter sand.
Backwash the filter (Section 6.2.5) at this point to remove fines;
drain down the filter and skim off the top 2.5 cm (I In.) of fines.
A makeshift fines scoop Is shown In Figure 48. Install the coal,
-------
INLET HOSE
WATER
i
FREEBOARD
60"
COAL 15"
I
I
12"
SAND i
j
TORPEDO SAHO
PEA GRAVEL
ff] GRAVEL *
#2 GRAVEL
SUPPORT AREA
t
^""^
1
[
2"
V
V
V
V
V
X
M
i'Vv. •..-.-;. ;^vv->£
.'.'•_•;;-.•• ;;'.'• •.-•'.••
Ill
i
\
/
^~
. — •
/
/ (AND BACKWASH
/THROUGH DISCHARGE LIN
/
^\_
f
?*
%
:-^£
?
**H
\
»
7
^
•T"^'"^
**$
^ " "*• ^'s -1 *
£Sfe[?^. '4
• . • . ' • -
^
\
\
"1
BRICK SUPPORTS
EVALUATION /5
50"
EXPANDED METAL
, GRATING
S
\
^- . TIE BOTTOM OF OUTLET
TO GRATE
V\
PLAN FOR PLACEMENT OF BRICKS
* DO NOT LET THE FREE DISCHARGE POINT EXTEND BELOW THE TOP OF THE BED
INCHES x 2.5* - cm
Figure A?. Construction details for filters.
-------
Table 25. COLUMN OPERATION
DISCHARGE LINE SIZING
Maximum Flow Line Size
1/min. GPM cm in.
11.36 3 2.54 1
37.85 10 3.81 1.5
83.27 22 5.08 2
189.25 50 7.62 3
i5 90 10.16 4
Based on maximum total length of discharge of
10 feet and head loss of 2 inches.
-------
n
BROOM HANDLE
HOSE CLAMP-
-4
OFFEE OR COKE CAN
HOSE CLAMP
HOSE CLAMP-
10SE CLAMP
COFFEE OR COKE CAN
Fiqure ^8. Fines scoop,
249
-------
backwash again, and remove 2.5 cm (I in.) of coat fines.
6. Construct a surge tank to dissipate the inlet velocity head and act
as a backwash trough. A good size would be 1/4-1/3 the filter dia-
meter and about 0.3 m (I ft) in height. The surge tank may be sup-
ported by cables suspended from the top of the filter. Locate the
bottom of the surge tank 0.6 m (2k in.) above the top of the fil-
ter bed as shown on Figure *»?• If a surge tank cannot be constructed,
place the inlet hose in a horizontal, tangential position to cause
velocity dissipation through swirl. This technique will help mini-
mize the boring out effect on the bed, which causes channeling of
flow with resulting poor filtration.
7> Install an equalization tank, any type, with the restriction that the
top of the vertical wall be lower than the filter discharge. If the
equalization tank is to double as a backwash storage tank, the
process volume should be at least 8.0 rn^per m of filter bed
(200 gal./ft2) to accommodate one backwash for a single filter.
Calibrate the volume of this tank, by calculations, and put a scale
on the inside wall showing 0,4 m3 or 100 gal. increments. This
calibration will permit proper flow during forward flow and backwash
modes.
6.2.5 Operational and Maintenance Steps
Forward Flow-
I. Set up the system in the forward flow mode as shown in Figure 46.
2. If backwash ing of fines was not performed, leaving the media in
submerged condition, care must be taken during filling, e.g., re-
duced flow rate so that the media is not bored out by the flow.
3- Throttle the inlet flow as necessary to achieve the desired filtra-
tion rate (I63j/min. (k gpm/ft2) is design rate). When flowing at
sq m
design rate, the water level should stabilize. Mark this level on
the tank wall as the clean bed head. If the water level is more
than 0.3 m (I ft) above the bed at design flow during the first
filter run, there is probably some blinding from fines taking place
and the fines removing procedure should be repeated. If, after
backwash, the clear bed head does not come back close to the clean
bed head, consult the troubleshooting section.
k. When the head rises to within 15 cm (6 in.) from the top of the
tank, either the flow rate must be reduced or the filter must be
backwashed.
250
-------
Backwash Mode (44)-
Set up the system for the backwash mode as shown in Figure 49.
Restrain the backwash waste suction hose so that it will not be
possible for it to become attached to the bottom of the surge
tank. This would starve the backwash waste pump and require
that it be shut off momentarily to release the hose.
Explanation; Backwashing of filters is intended to:
a. Remove undesirable fines during filter preparation.
b. Remove collected suspended materials.
c. Stratify the bed.
d. Remove air bubbles and pockets.
It is desired to backwash for a total of about ten to fifteen
minutes at: 4.1 m3/min (10 gpm/ft2),
m2 of filter
or a volume of about 41-61.5 m3/m2 (100-150 gal./ft.2)- The required
volume and flow rate are given in Figure 49* Flow setting may be
easier by noting the drop in level of the equalization tank.
Explanation; Efficient backwash requires that a certain flow
rate, termed the minimum fluidization velocity,
be passed upward through the bed causing all of
the media particles to separate.
Note whether the total bed is in agitation (de-
sirable)* Channeling is caused by poor back*
wash water distribution. Extended backwash
period may help to effect better removal in this
situation.
CAUTION; Do not allow an excessive flow rate to cause the media
" to be washed Into the effluent trough. If you are
in doubt as to whether this Is happening or not, take
a sample near the effluent trough with a glass jar
and visually inspect for media carry-over.
After the backwash Is completed the water above the bed should
appear to be clear and not murky. After the pump is turned off, a
short duration must be allowed for the water to syphon backward
through the backwash pump thus permitting the hose connection at
the filter discharge to be separated without having a back pres-
sure behind it.
251
-------
CO
1
o
<
CO
I
21,000
18,000
15,000
12,150
12,000
9,000
6,000
3,000
(GAL.)
- (5,548)
- (4,756)
-(3,963)
(3,170)
GPH L/Mln.
(370)
-(2,378)
"(1,585)
- (793)
(106) -
(53) -
1.400
1,200
1,000
810
800
600
400
200
,
(ft/) (o)
0.5
(5.4)
1.0
(10.8)
FILTER AREA
1.31 1.5
(16.1)
3-0
(21.5)
B
VOLUME BASED ON 15 MIN. BACKWASH
FLOW RATE BASED ON 611 1/mfn.
m
Figure 49. Backwash volumes for column processes.
252
-------
6.2.6 Filter Troubleshooting
I. Mudballing - In cases where a sllty water ts being filtered or oils
or greases are present, mud balls may form and gradually pass down-
ward through the bed during backwash. They tend to accumulate at
the media support and act to restrict flow. Mudballing may be
alleviated by air lancing. An air compressor of 0.28cum/mln.
(10 cfm) capacity Is connected to a straight 1.2 cm (0.5") tube. A
valve Is necessary to meter the flow of air through the tube.
The tube should be Inserted into the bed no further than the tor-
pedo sand layer 68.5 cm (27"). The bed must be covered with water
during air lancing but the backwash pump must be left off. The
tube is moved around to cover the entire bed area. The air
discharge should cause significant local turbulence. After the air
lancing procedure is completed, the bed must be backwashed before
being put back in operation.
2. Excessive Clean Bed Head - If backwashing and/or air lancing does
not permit return to the clean bed head, 2-5 cm (1-2 in.) of coal
may be removed and replaced. This procedure will be especially
effective if surface blinding is occurring.
3. Poor Effluent Quality - Suggests:
a. Too high a flow rate.
b. Poor fi1terabi1tty of the process flow.
c. Channeling of the bed (uneven distribution of flow)
d. Excessive intermixing of the media.
6.3 CARBON ADSORPTION
6.3.1 Process Description
Activated carbon adsorption is a physical phenomenon which removes organic
and some inorganic chemicals from water. These chemicals are physically ad-
sorbed on the large surface area of the carbon (typically 50Q-IOOO m^/gr).
The activated carbon can be produced from various cellulosic materials
including wood, coal, peat, lignin, etc. These are prepared using dehydra-
tion and carbonization, followed by activation to enlarge the pore openings,
which increases the surface area and therefore increases the adsorptive
capacity.
The adsorption process is dependent on the nature of the material being
adsorbed, the solution and the carbon used for adsorption. Critical factors
include molecular size and polarity, type of carbon, pH of the solution,
carbon contact time and solubility of the contaminant. The adsorption rate
increases with increasing temperature and decreasing concentrations. In
general, concentrations greater than 1000 mg/1 of soluble contaminant re-
quire excessive detention times and produce large amounts of spent carbon.
253
-------
The amount of carbon needed to adsorb a certain chemical must be established
by actual testing. Various tests can be used, but these should be done on
the contaminant in its natural environment since constituents of the medium
may also exert a carbon "demand". One test which can be run Is a carbon
isotherm. This test Indicates the amount of contaminant adsorbed per weight
of carbon at equilibrium conditions. However, since equilibrium conditions
are not met in the actual application, scale-up factors are required. Other
shorter tests compare adsorption of molecules on different types of carbon.
The Molasses number indicates a carbon's affinity for large molecules and
a Iodine number the affinity for small molecules (k$) . More information on
these tests is available in other sources
Once the capacity of the carbon has been reached, the carbon must be replaced
and the spent carbon disposed of or regenerated for reuse. Regeneration can
be done using various physical and chemical techniques. However, thermal
regeneration is the most common method. This process requires high tempera-
tures and a controlled atmosphere and is therefore unsuited for field imple-
mentation unless a preconstructed mobile system is available. Instead, carbon
should be removed and hauled to an established site for regeneration or in-
cineration.
Offstream treatment is typically done using either powdered or granular
carbon. Usually offstream treatment is performed in column tanks which
provide efficient use of the carbon in the system. Carbon columns are simi-
lar to filters in many ways:
I. Efficiency of the bed is dependent on good flow distribution which
will provide uniform contact time for the entire fluid stream.
2. An underdrain system is necessary to prevent the carbon from exiting
with the effluent water and to distribute backwash water.
3. Initial backwash is required to remove fines and air pockets, as well
as to stratify the bed.
In other ways, carbon columns are distinct from filter operations:
1. Termination of the cycle is established by "breakthrough" which in-
dicates that the adsorptive capacity of the bed has been reached.
Once spent, the carbon must be transported out of the bed and re-
placed with fresh media.
2. For efficient adsorption, the carbon must be "wetted" prior to use.
This process may require up to 2k hours at room temperature with the
carbon submerged in clean water (or less time at higher temperatures).
Therefore, a source of clean water must be available on site for use
in wetting the carbon prior to startup of the system.
3. Use of the carbon column as a filter causes inefficient use of the
adsorption capabilities. Therefore, clarification processes in-
cluding dual media filtration are necessary pretreatment steps prior
to carbon adsorption.
-------
k. Carbon columns possess more versatility than filters and can be
operated in either downfiow or upflow modes. Suspended solids are
not removed during upflow operation due to bed expansion and extra
contact time is generally necessary for this operation because of the
expanded bed condition.
When a carbon adsorption process is constructed in the field, the first,
priority is the ordering of carbon which may require a 2k to kB hour lead time
and an additional 2k hours to wet prior to use. The amount of carbon re-
quired is determined by the treatment specifications in Table 22. A range
of weight of carbon per weight of soluble contaminant is given to aid in
ordering the carbon. The following calculation should be done to determine
the amount of carbon needed.
Example A.
I. Spill of Parathion: l(r gal. of water
The solubility of Parathion is 2k mg/1
Pounds of soluble Parathton - 2k x B.3k x IP5 • 20.0 Ibs
(Ibs x .k$k = kg) I06
(gal. x 3-785 = 1)
Then, the range of carbon needed to remove parathlon Is 100-300 #/#
of soluble material. Therefore, the maximum number of pounds of
carbon Is 20.0 Ibs. of parathlon x 300 - 6,000 Ibs. of carbon. This
amount should be ordered.
Once the carbon is placed in the column, then the actual carbon requirement
of the system must be tested. Since it is recommended that the carbon colunns
be run in series with an equalization tank between, samples can be taken
periodically from the effluent lines of the columns, composited, and sent
the laboratory for analysis. These analyses will indicate when the first
carbon column has broken through and future carbon changes can be based on
that time period or additional sampling. The second column will allow the
operation to safely continue In the Interim until the samples can be analyzed.
When using powdered carbon during offstream operation, carbon can be injected
into a tank, mixed via hydraulic, air or mechanical means and then collected
prior to discharge of the wastewater. However, the carbon Is not used as
efficiently with this method, but the same weight of carbon should be initial-
ly ordered. As the carbon is spent, the data can be extrapolated and the
additional amount ordered.
6.3.2 Design of Activated Carbon Columns (k6_,__k7)_
I. Order the activated carbon using the formula presented In the process
description to determine the total amount of activated carbon re-
quired to treat the spill.
CAUTION; Due to the long times required to get the activated
carbon on site, it is essential that It be ordered
255
-------
immediately! If the total amount can not be obtained at once, have
the availabie weight shipped immediately.
2. Wet the activated carbon.
Explanation; The activated carbon should be deposited in hold-
ing tanks and sufficient water should be added
to cover the carbon with 6" or more of water.
CAUTION : This step Is essential for good removal rates
during operation of the activated carbon column.
3. Determine the required activated carbon bed surface area from the
process flow rate using Figure 50.
Explanation; Required carbon bed surface area Is based on a
design bed flow rate of
81.1,-1^1 - 2.0 gpm/ft2
m2
Operational ranges may vary from
M).7-81.A l/mtn (1-2 gpm/ft2)
m 2
Example; (From Figure 50) At 212 l/min, a bed area of 2.60 m
will be required.
Select a carbon column tank from Section 7-3 with the following:
a. A tank with vertical sides (Types A, F, G).
b. An above-ground tank.
c. A minimum height of 2.7 m (105 in)-
d. A diameter in the range of .6-1.2 m (2^-60 in).
Explanation: Over 1.2 m (60 in.) in diameter, a single
outlet will probably not be sufficient to
permit uniform flow distribution necessary
for adequate backwashing. Multiple outlets
would be required for these larger sizes
or the construction of a header lateral
system (not covered in these instructions).
e. A flat bottom which can be uniformly supported, e.g., laying
flat on the ground.
f. Tank wall construction which a hole may be machined for
an outlet.
256
-------
o
o
ftz m^
26.1 8
75.3
64.6
53.8
43-1
32.3
21.5
10.8
— 6
-5
-3
- 2
1
/
/
/
/
FLOW RATE
40.7 l/min/m2
(1.0 gpm/ft2)
(LONGER DETENTION
TIME)
\
/6>ERATIONAL RANGE
X
HIGH FLOW RATE
81.4 l/min/m2
(2 gpm/ft2)
(SHORTER DETENTION TIME)
1
1
1
I
l/min 50 100 150 200 250 300
gpm (13.2) (26.4) (39.6) (52.8) (66.0) (79-3)
FLOW RATE
Figure 50. Required surface area for carbon columns.
257
-------
5. Order gravel for media underdrains from a local sand and gravel yard
using amounts from Figure kS- Order equal amounts of pea gravel, and
#1 and #2 gravels, and one-half that amount of torpedo sand.
Explanation^
Example;
Pea gravel is about .3' cm (0.23 in.) in diameter;
#1 gravel ranges In size from 1.25"! cm (0. 5-0. 75
in.); #2 gravel ranges in size from 2.50-2.90 cm
(1.0-1.5 »n.).
(From Figure A5). For the flow rate of 212 l/min,
order the following quantities;
Torpedo Sand - 0.065 m3
Pea Gravel, #1 and #2 gravels - 0.132 m',
6.3.3 Construction Options for Activated Carbon Columns - Preferred option
Gravity Outlet (F I gure 51 ) Full gravitational flow, with a free discharge
leading to an equalization and backwash storage tank.
Explanation;
Advantages:
CAUTION;
Gravity flow rather than suction from a pump is desirable
to prevent air blinding of the bed.
Easy to operate and monitor effluent quality. Outlet lo-
cation permits bed to remain submerged after batch runs, a
desirable feature. Can be hydraulleally connected with
hoses and a total of six hose fittings; eliminating the
necessity of piping and valves.
In cases where hazard to personnel would exist from con-
tact with fluid, this option has a drawback in the neces-
sity to manually transfer hoses when shifting the forward
flow to backwash mode.
Two pumps may be used for handling both forward flow and backwash, provid-
ing the pump capacities are determined from backwash requirements and that
they can be throttled to accommodate forward flow and backwash flow condi-
tions. This option is well-suited to a parallel flow arrangement utilizing'
multiple activated carbon columns and a single equalization tank.
Explanation; The benefit derives from the fact that backwash flow rate
is four times forward flow rate. Thus, in a single
activated carbon column system both pumps operate in the
forward mode at 25% capacity. On the other hand, if say
two activated carbon columns are used, the pump could
operate at 50% capacity in forward flow, with the stipu-
lation that the activated carbon columns be backwashed
individually.
Any type tank may be used for equalization, in-ground or out, provided that
the wall height be lower than the activated carbon column outlet fitting
height.
258
-------
INFLUENT
PUMP
» I O
FORWARD FLOW MODE
CARBON COLUMN
DISCHARGE
PUMP
SURGE
TANK
EQUALIZATION
& BACKWASH STORAGE
BACKWASH
WASTE TANK
TO
SEDIMENTATION
BACKWASH MODE
BACKWASH WASTE
SUCTION HOSE
i
BACKWASH
SUPPLY PUMP
SURGE
TANK
Figure 51. Preferred option and operating modes - carbon adsorption
259
-------
6.3.4 Construction Steps for Activated Carbon Columns
Preferred Option - Gravity Outlet (Figure 52).
I. Construct tank shell and bottom as instructed in Section 7.3-3.
2. Install brick supports for an expanded metal grating underdrain
support. Note that all bricks are to be oriented radically with
the center of the column, except the bricks on the periphery.
For a one piece grating use about 12 bricks per square meter.
3. Install an expanded metal grating covering the complete column
area. The maximum opening in the grating shall not pass a 2.5 cm
(I In) sphere. Standard 3.0 lb., 4.0 Ib., or 5.0 lb., expanded
metal grating will meet this requirement. Construct from one
piece, if possible. If installed in multiple pieces, be sure the
free edges are supported sufficiently (almost continuous support).
Fit grating so that no holes over 2.5 cm (I in.) in diameter are
created.
4. Install the discharge line as shown, tied on one end to the grating
and extending through the tank wall at I.27 m (50 in.) above the
base of the column. Discharge line size is given in Table 25.
5. Install the gravel and sand underdrain layers.
6. Install 1.2 m (48") of activated carbon which has been wetted for 48
hrs (see Preferred Option Figure 51). Backwash the filter to
remove fines (see Sec n 2.5 for proper backwash method for
removal of fines). A makeshift fines scoop is shown in Figure 48.
Explanation: The carbon column sn^uld have 1.2 m (4 ft.) of
standing water before introduction of the carbon.
As this water Is displaced by carbon it should be
collected in the equalization basin. A mark 1.2 m
(48") above the torpedo sand will insure the
proper bed depth is obtained.
CAUTION; All lines in which activated carbon is to be pumped
must be at least 5cm (2 In.) in diameter. The lines
must be kept as short as possible, i.e., the suction
line is not to exceed 6m (20 ft.) and the discharge
line will be no longer than necessary.
Wetted activated carbon can also be installed by hand using buckets
and shovels, etc.
7. Construct a surge tank to dissipate the inlet velocity head and
act as a backwash trough. A good size would be 1/4 - 1/3 the
column diameter. The surge tank may be supported by three cables
suspended from the top of the column. Locate the bottom of the
260
-------
INLET HOSE
y
| CARBON
1 1
TORPEDO SAND j 2
PEA GRAVEL j | A
#1 GRAVEL I | 4
#2 GRAVEL | 4
SUPPORT AREA ! A
EXPANSION
HE GHT
^
SURGE TAN
S
K
FREEBOARD
"X
u
FREE
DISCHARGE
POINT*
6
EXPANDING
METAL
GRATING
105
(A 1
BRICK SUPPORTS
TIE BOTTOM OF OUTLET
TO GRATE
EVALUATION VIEW
inches x 2.51* - cm
PLAN VIEW FOR BRICK PLACEMENT
* DO NOT LET FREE DISCHARGE POINT EXTEND BELOW THE TOP OF THE BED.
Figure 52. Carbon column construction details.
261
-------
surge tank .6 m (24 in.) above the top of the column bed as shown
on Figure 52. If a surge tank cannot be constructed, place the
inlet hose tn a horizontal, tangential position to cause velocity
dissipation through swirl. This technique will help minimize the
boring out effect on the bed, which causes channeling of flow.
8. Install an equalization tank, any type, with the restriction that the
top of the vertical wall be lower than the column discharge. The
process volume should be at least 8.0 m' per m^ of column (200 gal./
ft?) to accommodate one backwash for a single column. Calibrate the
volume of this tank, by calculations, and put a scale on the inside
wall showing 0.5 m3 or 100 gal. increments.
Explanation; This calibration will assist In flow setting.
6.3.5 Operational and Maintenance Steps for Activated Carbon Column Forward
Flow
I. Set up the system in the forward flow mode as shown in Figure 51•
2. If backwashing of fines was not performed during or after column
construction, care must be taken during filling, e.g., reduce
flow rate so that the media Is not bored out by the flow.
3. Throttle the Inlet flow as necessary to achieve the desired flow
rate.
8| «, '/"in. (2 gpm/ft2)
m2
When flowing at design rate, the water level should stabilize. Mark
this level on the tank wall as the clean bed head. If the water
level is more than .3 m (I ft.) above the bed at design flow during
the first column run, there is probably some blinding from fines
taking place and the fines removing procedure should be repeated.
If, after backwash, the clear bed head does not come back close to
the original level, consult the troubleshooting section.
k. Sample frequently at the effluent from each column or in the equali-
zation tank. Have analysis done to establish effective loading
possible for that carbon. When carbon has broken through, replace
It immediately.
5. Activated carbon columns should never become fouled. If they do, the
processes prior to the activated carbon column should be inspected
and steps should be implemented to improve the product water of the
processes. If the head rises to within 15 cm (6 in.) from the top
of the tank, the column must be backwashed. However, backwashing is
undesirable, because stratification of the carbon bed will occur,
and should not be done unless absolutely necessary.
262
-------
Backwash Mode
I. Set up the system for the backwash mode as shown tn Figure 51 •
Restrain the backwash waste suction hose so that It will not be
possible for it to become attached to the bottom of the surge tank.
This would starve the pump and require that it be shut off momen-
tarily to release the hose.
Explanation: Backwash ing the carbon column is intended to:
a. Remove undesirable fines during filter preparation;
b. Remove air bubbles and pockets during filter preparation;
c. Remove collected suspended material.
2. Backwash Ing during carbon column preparation or for removal of fines
and air bubbles and pockets: It is desirable to backwash for a total
of 15 minutes at
-0 1/min. (O.JI* gpm/ft.2)
m2 of Filter
The accepted operational range for carbon column preparation back-
washing Is
20.4 to 40.7 1/mtn-
,
m of Filter
The required volumes and flow rates or carbon column preparation are
given In Figure 53. Flow setting may be easier by noting the drop
in level of the equalization tank.
2
CAUTION; Flow rates In excess of 40.7 l/mln./ra may cause the
activated carbon to stratify thus decreasing Its abi-
lity to adsorb contaminants.
3. Backwashing for removal of suspended materials from the carbon column:
It is necessary to backwash for about 10-15 minutes at
, . m^/min, _ (150 gpm/ft.2)
O.I 2 "~ -
m of Filter
The required volume and flow rates are given In Figure 53. Flow
setting may be easier by noting the drop in level of the equaliza-
tion tank.
263
-------
CM
(Total)
GPM
4.5
4.0
3.4
ID
LU
£
o 2.8
in
§ 2-3
2
1.7
1.1
0.51
c
•M*
E
CM
(Total)
(Gal.)
COLUMN AREA
VOLUME IS BASED ON A 15 MINUTE BACKWASH
RECOMMENDED BACKWASH RATES ARE FROM
40.7 L/min/m2 to 20.35 L/min/m2
L/min/m2 *1 GPM/ft2vb
60 (222.4)
PREFERRED RATE
30 L/min/m (0.74 GPM/ft
50 (189.5
40 (151.6)
OPERATIONAL
RANGE
30 (113.7)
20.35 L/min/m (0.5 GPM/ft )-
(75.7)
(37.8)
Figure 53. Carbon bed preparation by backwashing for fines removal
-------
5.
Explanation: Efficient backwash requires that a certain flow
rate termed the minimum fluidlzation velocity
be passed upward through the bed causing all of
the media particles to separate.
CAUTION; Do not allow an excessive flow rate to cause the
activated carbon to be washed Into the effluent
trough. If you are in doubt as to whether this
is happening or not, take a sample near the ef-
fluent trough with a glass jar and Inspect for
activated carbon carry-over.
Note whether the total bed is in agitation (desirable) or if the
flow is being channeled (undesirable). Channeling is caused by
poor backwash water distribution. Extended backwash period may
help to effect better removal in this situation.
If backwashing does not effectively remove the suspended material
or if extreme stratification occurs, the carbon must be replaced
prior to further column use.
CAUTION; If backwash!ng at high rates above
A0.7 1/mtn (2.0gpm/ft2)
m2 of Filter
is performed, removal rates of the hazardous material may
be significantly lowered.
After the backwash is completed the water above the carbon bed
should be clarified and not murky. After the pump Is turned off,
a short duration must be allowed for the water to syphon backward
through the backwash pump thus permitting the hose connection at
the filter discharge to be separated without having a pressure be-
hind it.
Any fines should then be skimmed from the bed.
Removal of the exhausted activated carbon: The preferred removal
method for the spent activated carbon is shown in Figure 5k, The
carbon should be submerged prior to and during removal.
Explanation:
CAUTION:
Because activated carbon will dewater freely, it
Is necessary to pump water into column to keep the
activated carbon slurried. The water can be re-
placed by intermittent operation of the backwash
system or auxiliary pumps can be used to pump
product water into the top of the column.
Do not remove too much carbon or the underdrain
265
-------
INLET PIPE
1
WATER i
. ,.
SLURRY PUMP
r^K
t
i
UNDERDRAIN
\ <
OVERFLOW PIPE
1
WET
MEC
4
r
TED
IIA
> J
kLIN
THA
E LESS
N 20* LONG
SPENT MEDIA
HOLDING TANK
EQUALIZATION BASIN OR
SPECIAL TANK FOR WETTED MEDIA
INLET PIPE
DISCHARGE
f
FLOODED COLUMN
UNDERFILTERS
WATER
MAKEUP PUMP
LINE
PRODUCT
WATER TANK
Figure 5^. Operating modes for carbon transfer
266
-------
will be disturbed. To avoid this, it is pre-
ferred to leave an inch or two of carbon above
the torpedo sand layer.
6.3*6 Activated Carbon Column Troubleshooting
I, Excessive Clean Bed Head - If backwashing does not permit return
to the clean bed head, surface blinding may be occurring which
can be alleviated by removing and replacing the top 5-12 cm
(2-5 in.) of carbon from the bed. If suspended material is clog-
ging the column, steps should be implemented to Improve the
feed water quality.
2. Poor effluent quality suggests:
a. Too high a flow rate;
b. Channeling of the bed (uneven distribution of flow);
c. Excessive mixing of media;
d. Exhausted activated carbon.
6.A ION EXCHANGE
6.k.I Process Description
Ion exchange is a process in which ions held by electrostatic forces to
functional groups on the surface of a solid are exchanged for ions of a
different species in solution (43). This process takes place on a resin
which is usually made of a synthetic material. The resin contains a
variable number of functional groups which establish both the capacity of
the resin and the type of group removed. Various kinds of resins are
available Including weakly and strongly acidic cat Ionic exchangers and weak-
ly and strongly basic anion exchangers. The ions are exchanged until the
resin is exhausted and then the resin is regenerated with a concentrated
solution of ions flowing in a reverse direction. Various specific reactions
occur but generally the reaction is as follows:
Rl + l< >RI + I
x c ex
R = resin
I = exchangeable ion
4\
I « contaminating ion
The ion exchange process Is dependent on the type of resin involved, the
specificity of the resin and the general ion content of the wastewater.
Capacities of resins also vary with the manufacturer of the resin, the dis-
tribution of flow and concentration of contaminant.
267
-------
The amount of resin required must be established by chemical tests done on
wastewater for ton content. The best type of resin to use is established
mainly by the specific contaminant to be removed, the amount of wastewater
involved and the other ionic demand on the resin. A resin manufacturer must
be contacted by the OSC to allow the correct resin to be chosen. The
following information must be given to the manufacturer.
I. Name of compound to be removed,
2. Concentration of contaminant,
3> Amount of wastewater to be treated,
1». Chemical analysis of ions.
Cation removal
(e.g. Metal s/NHi,) * An ion removal
a. Hardnessa- Chloride
b. Sodium b. Sulfate
c. Other cations c. Nitrates
d. Other significant anions
The resin manufacturer can then specify the amount and type of resin required
to remove the entire contaminant from the waterway. Unless absolutely
necessary, the resin will not be regenerated on site; once the capacity is
depleted, the resin will be replaced, hauled away for regeneration and
either returned for reuse on site or sent to storage.
Two types of off-stream treatment are available, I) column exchange and 2)
distribution of uncontained media into a tank. Column treatment is more
common and more efficient. There are many similarities between ion ex-
change and carbon columns and some similarities to filters. The three sys-
tems have the following features in common:
I. Efficiency of the bed is dependent on good flow distribution which
will provide uniform contact time for the entire fluid stream.
2. An underdrain system is necessary to prevent the media from exiting
with the effluent water and to distribute backwash water.
3. Initial backwash is required to remove fines and air pockets, as
well as to stratify the bed.
The carbon and Ion exchange systems are similar in the following ways:
I. Termination of the cycle is established by "breakthrough" which
indicates that the exchange capacity of the bed has been spent.
This procedure is indicated by an increase in the concentration of
the contaminant to be removed or by a change in pH (when
strongly anionic or cat ionic resins are involved).
268
-------
2. Use of the column as a filter causes inefficient use of the ex-
change capabilities. Therefore clarification processes including
dual media filtration are necessary pretreatment steps.
3* Backwash(ng of these systems can be done, however, it is not
recommended and the necessity of frequent backwash ing indicates the
malfunction of upstream processes.
However, ion exchange does have a high potential for fouling since the size
of the resin particles is approximately the same as that of filter sand.
The amount of resin and the type required are established by the manufacturer.
However, the design of the columns presented in this manual is based on
two resins. Amberlite IRC-8^ and IR-120, The OSC must compare the critical
design data and then make appropriate changes in the design. (See Table 26).
TABLE 26. DESIGN PARAMETERS USED FOR ION EXCHANGE C»9)
Parameter
Loading rate
Loading range
Minimum bed depth
Expanded height
Head loss (total head
loss based on exp.
height)
Backwash rate
Backwash rate (range)
Design
metric
01 i. 1/mln
1,0.7 - 203.5 i^1
61 cm
43.2 cm 65%
0.07 kg/cm2
m
244.2 1/min
2
162.8-488.4 1/min
cr i teria
Engl ish
2
2 gpm/ft
1-5 gpm/ft2
24"
17"
0.69 ft of H20
ft
6 gpm/ft2
4-12 gpm/ft2
Backwash time
Backwash expansion
15 min.
58.4 cm, about 50%
15 min.
23", about 50%
269
-------
6.A.2 Des|gn for Ion Exchange Columns
I. Order the ion exchange media by contacting a manufacturer and
giving him the wastewater characteristics indicated in the pro-
cess description. See Section J.k for supplier.
Explanation? Due to long lead times to receive the resin on
site, it is essential to order the resin immedia-
tely. It is assumed that the resin will not
be regenerated in the column or on site due to
other hazards. Therefore, the amount of resin
ordered must have capacity to handle the entire
spill without regeneration.
2. Determine the required surface area from the process flow rate
using Figure 55.
Explanation: Required surface area is based on a design flow
rate of 81.A l/mln/mz(2.0 gpm/ftz)
Operational ranges may vary from 1»0.7~203.5 l/mln. (1-5 gpm/ft2)
m2
Example; (From Figure 55)• At 212 l/min., a bed area of
2.6 m2 will be required if the Ion exchange
column is to be run at B\.k l/min.
m2
3. Select a tank from Section 7-3 with the following:
a. A tank with vertical sides (Types A, F, B).
b. An above-ground ta/ik.
c. A minimum height of 3-2 m (127 In.).
d. A diameter In the range of 0.6-1.2 m (2A-60 In.).
Explanation; Over 1.2 m (60 in.) in diameter, a single
outlet will probably not be sufficient
to permit uniform flow distribution
necessary for adequate backwashIng.
e. A flat bottom which can be uniformly supported, e.g., laying
flat on the ground.
f. Tank wall construction In which a hole may be machined for
an outlet.
4. Order gravel for media underdralns from a local sand and gravel
270
-------
NJ
—J
UJ
ac
ec
3
to
o
o
C3
o
X
10.8 U
I/min 0
gpm 0
50 100 150 200 250 300 350 kOO k$0
(13.2) (26.k) (39.6) (52.8) (66) (79.2) (32.k) (105.6) (1(8.8)
3BASED ON A FLOW OF 2 gpm/ft2.
Figure 55- Required surface area for ion exchange columns.
-------
yard using amounts from Figure A5. Order equal amounts of pea gra-
vel, and #1 and #2 gravels, and one-half that amount of torpedo
sand.
Explanation:
Pea gravel Is about .31 cm (0.23 in.) in diameter;
#1 gravel ranges In size from I. 25-1 f 9 cm (0.5"
0.75 In.); #2 gravel ranges in size from 2.50-3-90
cm (1.0-1.5 in.).
Example; (From Figure kS) • For the flow rate of 212 l/min.,
and the area requirement of 2.6 m2 order the fol-
lowing quantities:
Torpedo Sand - 0.15 m^
Pea Gravel, #1 and #2 gravels - 0.31 m^.
6.*>.3 Construction Options for Ion Exchange Columns
Preferred Option - Gravity Outlet (Figure 56)
Fully gravitational flow, with a free discharge leading to an equalization
and backwash storage tank.
Explanation; Gravity flow rather than suction from a pump Is desirable
to prevent air blinding of the bed.
Advantages; Easy to operate and monitor effluent quality. Outlet
location permits bed to remain submerged after batch runs,
a desirable feature. Can be hydraut icat ly connected with
hoses and a total of six hose fittings; eliminating the
necessity of piping and valves.
CAUTION; In cases where hazard to personnel would exist from con-
tact with fluid, this option has a drawback in the neces-
sity to manually transfer hoses when shifting from the
forward flow to backwash mode.
Two pumps may be used handling both forward flow and backwash, providing the
pump capacities are determined from backwash requirements and that they
can be throttled to accommodate forward flow and backwash flow conditions.
This option is well-suited to a parallel - flow arrangement utilizing mul-
tiple ion exchange resin columns and a single equalization tank.
Explanation;
The benefit derives from the fact that backwash flow rate
is four times the forward flow rate. Thus, in a single
Ion exchange column system, both pumps operate In the for-
ward mode at 25% capacity. On the other hand, if say two
ion exchange columns are used, the pump could operate at
50% capacity in forward flow, with the stipulation that
ion exchange columns be backwashed individually.
272
-------
FORWARD FLOW MODE
INFLUENT PUMP
EXCHANGE COLUMN
DISCHARGE
PUMP
SURGE
TANK
EQUALIZATION AND
BACKWASH STORAGE
BACKWASH
WA$I£_IANK
TO
SEDIMENTATI
BASIN
BACKWASH MODE
BACKWASH
WASTE
ASUCTION
HOSE
BACKWASH
SUPPLY PUMP
SURGE
TANK
Figure 56. Preferred option and operating modes - ion exchange
273
-------
Any type tank may be used for equalization, in-ground or out, provided that
the wall height be lower than the ton exchange column outlet fitting height.
6.4.4 Construction Steps for ion Exchange
Preferred Option • Gravity Outlet (Figure 57).
I. Construct tank shell and bottom as instructed in Section 7.3.3.
2. Install brick supports for an expanded metal grating underdrain
support. Note that all bricks are to be oriented radially with
the center of the column, except the bricks on the periphery. For
a one piece grating use about 12 bricks per square meter.
Explanation: During backwash the distribution of water In the
underdrain area is critical. Symmetrical orien-
tation of bricks assists in backwash flow dis-
tribution.
3. Install an expanded metal grating covering the complete column area.
The maximum opening in the grating shall not pass a 2.5 cm (I in.)
sphere. Standard 3.0 Ib., 4.0 Ib., or 5*0 lb., expanded metal
grating will meet this requirement. Construct from one piece if
possible. If Installed in multiple pieces, be sure the free edges
are supported sufficiently (almost continuous support). Fit grating
so that no holes over 2.5 cm (I in.) in diameter are created.
4. Install the discharge line as shown, tied on one end to the grating
and extending through the tank wall at 1.83 m (72") above the base
of the column. Discharge line size is given in Table 25.
5. Install the gravel underdrain layers.
6. Install 61 cm (2k in.) of ion exchange resin (see preferred option
Figure 57). Backwash the column to remove fines (see section
6.2.5 for proper backwash method for removal of fines).
Explanation; The ion exchange column should have 0.6 m (2 ft.)
of standing water before introduction of the re-
sin, as this water is displaced by the resin it
should be collected in the equalization basin.
A mark 61 cm (24 In.) above the torpedo sand
will insure the proper bed depth is obtained.
CAUTI ON: All lines in which ion exchange resin is to be
pumped must be at least 5 cm (2 in.) In diameter.
The lines must be kept as short as possible, i.e.,
the suction line Is not to exceed 6 m (20 ft.)
and the discharge line will be no longer than
necessary.
21k
-------
INLET HOSE
in.
ION EXCHANGE
RESIN
2k
TORPEDO SAND,
PEA GRAVEL 1 !
#1 GRAVEL
#2 GRAVEL
SUPPORT AREA
SURGE TANK
FREEBOARD
EXPANSION
HEIGHT
1 'l "Vs
I" ' ' 1 I Ml FT
FREE DISCHARGE
POINT *
MINI HUM
BRICK SUPPORTS TIE BOTTOM OF OUTLET
TO GRATE
EVALUATION VIEW
INCHES x 2.54 - cm
PLAN VIEW FOR BRICK PLACEMENT
* DO NOT LET FREE DISCHARGE POINT EXTEND BELOW TOP OF BED
Figure 57- Ion exchange column construction details.
275
-------
Ion exchange resin can also be installed by hand using buckets and shovels,
etc.
7. Construct a surge tank to dissipate the inlet velocity head and
act as a backwash trough. A good size would be IA - 1/3 the
column diameter. The surge tank may be supported by three cables
suspended from the top of the column. Locate the bottom of the
surge tank .6 m (24 in.) above the top of the column bed (as
shown in Figure 57). If a surge tank cannot be constructed, place
the inlet hose in a horizontal, tangential position to cause
velocity dissipation through swirl. This technique will help
minimize the boring out effect on the bed, which causes channel-
ing of flow.
8. Install an equalization tank, any type, with the restriction that
the top of the vertical wall be lower than the column discharge.
The process volume should be at least 3.7 m* per m2 of column
(291 gal/ft2) to accommodate one backwash for a single column.
Calibrate the volume of this tank, by calculation, and put a scale
on the inside wall showing 0.5 m3 or 100 gal. increments.
Explanation; This calibration will assist in flow setting.
6.4.5 Operational and Maintenance Steps for Ion Exchange
Forward Flow
I. Set up the system In the forward flow mode as shown in Figure 56.
2. If backwashing of fines was not performed during or after column
construction, care must be taken during filling, e.g., reduced
flow rate so that the media is not bored out by the flow.
3. Throttle the inlet flow as necessary to achieve the desired flow
rate (81.4 l/mtn. (2 gpm/ft2) is design rate). When
m2
flowing at design rate, the water level should stabilize. Mark
this level on the tank wall as the clean bed head. If the water
level is more than .3m (I ft.) above the bed at design flow during
the first column run, there is probably some blinding from fines
taking place and the fines removing procedure should be repeated.
If, after backwash, the clear bed head does not come back close to
the original level, consult the troubleshooting section.
k. Monitor the pH of the effluent which flows either into or from
the gravity equalization tank. When the pH changes drastically from
the normal operating value the resin is exhausted and flow must
then be stopped and the resin replaced.
276
-------
5. Ion exchange columns should never be allowed to become fouled. If
they do,the processes prior to the Ion exchange column should be
Inspected and steps should be Implemented to Improve the product
water of these processes. If the head rises to within 15 cm
(6 In.) from the top of the tank.it is time to backwash, which is
undesirable.
Backwash Mode
I. Set up the system for the backwash mode as shown in Figure 56.
Restrain the backwash waste suction hose so that It will not be
possible for It to become attached to the bottom of the surge tank.
This would starve the pump and require that It be shut off
momentarily to release the hose.
Explanation; Backwashing the Ion exchange column Is intended to:
a. Remove undesirable fines during filter
preparation;
b. Remove air bubbles and pockets during
filter preparation;
c. Remove collected suspended material.
2. For ion exchange column preparation, removal of fines, air bubbles
and pockets and suspended material removal, it is desirable to
backwash for a total of 15 minutes at 244.2 I/min^
m2 of filter
(6.0 gpm/ft2). The accepted operational range for ion exchange
column preparation backwashIng is 162.8 to 488.4 1/mJru
«
m of area
(4.0 - 12 gpm/ft2). The required volumes and flow rates for ion
exchange column preparation are given in Figure 58. Flow setting
may be easier by noting the drop in level of the equalization tank.
Explanation; Efficient backwash requires that a certain flow
rate termed the minimum fluidlzation velocity be
passed upward through the bed causing all of the
media particles to separate. Note whether the
total bed is in agitation (desirable) or if the
flow is being channeled (undesirable).
Channeling is caused by poor backwash water
distribution. Extended backwash period may
help to effect better removal In this situation.
CAUTION; Do not allow an excessive flow rate to cause
the ion exchange resin to be washed into the
effluent trough. If you are in doubt as to
whether this Is happening or not, take a
277
-------
<
ac
I
o
m
TOTAL
CUM
/4.0 -
2.8 -
2.3 -
1.7 ~
0.57 -
TOTAL
GAL.
I ,200
1,050
900
750
600
300
150
ft'
0.5
(5.4)
1.0
(1,0.8)
1.5
(16.2)
2.0
(21.6)
o
>
X
o
s
AREA OF EXCHANGE COLUMN
Figure 58. Backwash volume for Ion exchange.
278
-------
sample near the effluent trough with a glass jar
and Inspect for Ion exchange resin carry-over.
As an alternative to backwash ing, the Ion exchange bed may be re-
placed. This would be desirable If the exchange capacity Is al-
most exhausted.
3. After the backwash is completed the water above the bed should be
clarified and not murky. After the pump is turned off, a short
duration must be allowed for the water to syphon backward through
the backwash pump thus permitting the hose connection at the filter
discharge to be separated without having a pressure behind it.
Any fines should then be skimmed from the bed, and make-up resin
should be pumped into the bed to replace the resin that was removed.
A. Removal of the exhausted ion exchange resin: The preferred re-
moval method for the spent resin Is shown In Figure 59. The resin
should be submerged prior to and during removal.
Explanation: Because ion exchange resin will dewater freely,
it is necessary to pump water into the column
to keep the resin slurried. The water can be
replaced by intermittent operation of the
backwash system or auxiliary pumps can be used
to pump product water into the top of the column.
CAUTION; Do not remove too much ion exchange resin or the
underdrain will be disturbed. To avoid this it
is preferred to leave an inch or two of resin
above the torpedo sand layer.
.6 Ion Exchange Column Trouble Shooting
I. Excessive clean bed head - If backwashIng does not permit return to
clean bed head, 5-12 cm (2-5 in.) media may be removed and replaced.
This procedure will only be necessary If feed water quality is
high in suspended material which is causing surface blinding. If
suspended material Is clogging the column, steps should be im-
plemented to improve the feed water quality.
2. Poor effluent quality - suggests:
a. too high a flow rate (insufficient detention time);
b. channeling of the bed;
c. exhausted ion exchange resin;
d. improper choice of resin - wrong type of an Ion/cat Ion
removaI.
279
-------
INLET PIPE
SLURRY PUMP
,
WATER '
r
1
r
i
UNDERDRAIN
•4 <
OVERFLOW PIPE
i
^
r
WETTED
MEDIA
) J
kLIN
THA
E LESS
N 20' LONG
EQUALIZATION BASIN OR
SPECIAL TANK FOR WETTED MEDIA
INLET PIPE
DISCHARGE
i
FLOODED COLUMN
UNDERFILTERS
SPENT MEDIA
HOLDING TANK
LINE
WATER
MAKEUP PUMP
PRODUCT
WATER TANK
Figure 59. Operating modes for ton exchange resin transfer
280
-------
6.5 GRAVITY SEPARATION
6.5.1 Process Description
Gravity separation involves the removal from the water column of materials
with a different specific gravity than water. Both flotation and sedimenta-
tion processes are included as an off-stream treatment system. In situ
treatment is generally not applicable since dredging and absorbant processes
have been covered in Section 4.3.
Sedimentation: Sedimentation is the removal of solid particles from a
suspension through gravity settling (50). The process is used as a pre-
treatment and concentration step to reduce the load on downstream processes
and utilize the natural concentrating procedure. Various factors affect
the rate of settling including particle size and shape, density and visco-
sity of the water and other materials in the water column. The rate of
settling can be predicted using theoretical equations, however, a field
testing procedure is faster and more accurate.
Gravity separation has been included either as a necessary or optional
process in all of the treatment schemes. The requirement for sedimentation
preceeding the system is determined by the nature of the spill situation.
A large amount of suspended solids in the influent, a strongly insoluble
contaminant or sensitive downstream processes may lead to the use of a
sedimentation system. Each situation must be evaluated on Its own merits.
Criteria are listed in Section 6.5«3*
Several problems'are inherent when using sedimentation processes. The
first difficulty is that the batch nature of the process requires a bank
of parallel tanks to produce a continuous flow system. The number of
tanks is dependent on the fill and draw rate, the detention time of
settling and the amount of desJudging required.
The desludging operation is tedious, ttme consuming, can be dangerous to
personnel, and should be done as infrequently as possible. To reduce the
amount of desludging, a presettler can be used which is set up for contin-
uous desludging. The frequency of desludging is dependent on the
nature of the sludge produced, the removal device and the type of tank used.
The tank operation Is accomplished by:
I. Filling the tank up to the freeboard level by pumping fluid into
the influent well. The well dissipates the velocity head and
allows the fluid to overflow Into the tank without disrupting
the sludge blanket.
2. Allowing sufficient detention time for settling after filling
operation is completed.
3. Drawing off supernatent by manually controlled suction hose
which draws off the clear supernatent to the point where there
281
-------
is danger of sludge entering the suction hose. After drawoff,
tank refilling or desludging may proceed.
k. Removing sludge when a blanket has formed which has reduced the
batch size substantially. Desludging is performed with a solids
handling pump and special suction fitting.
There is an experimental settling test which can be used to establish flow
rates and number of tanks for sedimentation. It is mandatory that a mixed
sample of the wastewater be used to evaluate the settling capabilities.
The sample is placed in a cylinder and the position of the interface with
time is recorded. This data is then translated into a settling rate and
evaluated. If the settling rate is less than .031 mpm (0.1 fpm) then
chemicals may be added to increase the settling rate. The chemicals are
added, mixed and flocculated, then the clumped solids are allowed to settle.
There are several commonly used chemicals including ferric chloride, alum,
and polyelectrolytes. The following paragraphs describe these chemicals
and their use.
Ferric chloride: This compound is effective In clarifying both organic
and Inorganic suspensions. The final pH should be above 6 for best re-
sults so lime or caustic soda may be needed to control pH. Dilute sus-
pensions require dosages of approximately 50-500 mg/1 although larger
dosages may be needed for concentrated or highly alkaline suspensions. If
the wastewater is low in alkalinity, lime or caustic may be needed to raise
the pH to 6 or higher. Excessive doses of ferric chloride will result in
a brown colored effluent and should be avoided.
Alum: Aluminum sulfate is effective in clarifying both organic and in-
organic suspensions. The pH should usually be controlled in the range of
6.5 to 7*5 pH and this control is generally crucial for good alum use. If
a dilute suspension is to be treated, alum dosages of 100-1000 mg/1 should
be effective. Huge dosages may be needed for concentrated or highly alka-
line suspensions. As with ferric chloride, suspensions low in alkalinity
may require an addition of lime or caustic to produce the final pH range
of 6.5 to 7-5
Organic Polyelectrolytes: Polyelectrolytes are available in anionic,
cationlc or nonionic form and may be effective alone when flocculating sus-
pensions of inorganic materials (clay, soils, colloidals, metal salts
etc). These polyelectrolytes are usually not effective alone when floc-
culating organic suspensions, but can be used with alum or ferric chloride
for treating organic suspensions. Polyelectrolyte dosages vary with both
the type of charge on the polymer and the type of suspension to be
treated. Cationic polyelectrolytes are generally added in higher dosages,
1-10 mg/1 in dilute situations (less than 100 mg/1 suspended solids) and
anionic or noniqhic polymers are added at approximately 0.5 to 5 mg/1.
When the solution is concentrated and the suspended solids concentration is
greater than 1,000 mg/1 add 1-300 mg/1 of a catonic polyelectrolyte or
1-100 mg/1 of an anionic or nonionic compound.
282
-------
These chemicals are also used In combinations and various types of mixtures
should be evaluated prior to establishing the treatment mechanism. When
the chemicals are added, mixed and flocculated, the resulting solution and
solids should be examined for the following:
a. A relatively clear internatant (i.e., the liquid between the par-
ticles). A cloudy fnternatant may indicate the need for more
chemicals.
b. A medium to large but well defined floe. This is a good sign of
correct chemical dosages.
c. Initial settling of the fioc - the faster the floe drops out the
better-
d. A relatively small sludge volume (3~5%) - even In a 100 ml graduate
an approximate idea of sludge volume can be obtained. Excessive
volumes of sludge from chemicals Indicate future problems - a
different chemical or smaller dosage may be desirable.
The following paragraphs describe the uses of the treatment chemicals to
aid sedimentation. The total flocculation times are for full scale use.
Laboratory times for mixing are 15*30 sec. and for flocculation are 30
sec. to 2 minutes.
Polyelectrolytes: Slowly add polyelectrolyte solutions to the waste while
vigorously mixing the wastewater. Mix rapidly for I to 2 minutes to
ensure dispersal. Then agitate the material at a speed just sufficient to
keep the floe from settling and continue for 5 to 10 minutes. If more
time Is needed, increase the polymer dosage.
Alum Treatment: The order of addition of alum and then lime or NaOH may be
critical. However either alum addition first or last may be the best for
a given situation. Generally, alum addition followed by lime or NaOH
addition will give satisfactory results and allows simple pH control. Alum
should be added, mixed I to 2 minutes and then the lime or caustic can be
added to achieve the proper pH. Again flocculation speed Is established
at the rate to keep the floe in suspension. The flocculation time should
range from 5-15 minutes and if longer times are required, Increase the
alum dosage. If the floe is easily broken, add a polyelectrolyte to in-
crease the strength.
Alum and polyelectrolytes: The use of polyelectrolyte will allow a stronger
floe and a faster settling rate. Add the alum and lime or caustic as
described previously. Flocculate from 2 to 5 minutes to allow creation
of the desired alum floe. Then add polyelectrolyte in concentrations from
I to 10 mg/t. Increase the rate of agitation during polymer addition to
prevent settling and mix about I minute. Flocculate for 5*10 minutes or
increase dosage of polyelectrolyte.
283
-------
Ferric Chloride: (lime or caustic may be needed for pH control). Add
ferric chloride and then mix for 2 to 5 minutes vigorously. Then add
lime or caustic to raise pH to the desired level, mix an additional 2 to
5 minutes and then reduce mixing speed to allow flocculation. Flocculate
at a sufficient speed to keep floe from settling for 5 to 15 minutes.
If additional time is necessary, Increase dosages or add polyelectrolyte.
Ferric chloride and polyelectrolyte: Use the same procedure as ferric
chloride addition. After the second 5 minutes mix and add the poly-
electrolye (1-10 mg/1). Mix at a higher rate to prevent settling and
continue to mix approximately one minute. Then flocculate 5 to 10
minutes.
Once the chemicals and dosages have been determined, the system can be
operated. To establish the efficiency of the unit, sampling should be
done at both the influent and effluent of the batch and if the system is
not operating properly, further bench tests may be needed.
Flotation: Flotation is used to separate materials with a specific gravity
less than water. The contaminant rises to the top and is skimmed off
periodically. This skimming process should be done during each batch, so
the influent and effluent flows remain constant and do not disturb the
downstream processes.
The flotation process operation has the same basic steps as are used in
sedimentation except that skimming of floating substances Is performed
during each batch. A settled sludge blanket would probably accumulate
but typically in far less proportions than in the sedimentation tank.
Flotation rates can be either calculated methematically or measured In the
field. The equation for rise rate Is dependent upon the specific gravity
and viscosity of the water, the specific gravity of the particle, and the
estimated diameter of the globule. It Is commonly assumed that the dia-
meter is equal to 0.015. The rise rate is then equal to:
v = 0.02A1 iSw " Sr.) v - m/sec
t u t
Sw " sp.gr. of water
Sc = sp.gr. of contaminant
u = viscosity of water
The other method Is measuring the rising position of the Interface with
time, In the same manner as a solids settling test. Once the rate is
determined, the detention time is calculated:
Detention time » heIght of tank ?A (2 is a safety factor)
rise rate
Once the detention time is calculated, the test can be re-done for that
28k
-------
length of time and the scum volume estimated. The same chemicals and
dosages used for settling tests can be used for gravity flotation.
6.5«2 Bench Testing Procedure - Gravity Separation
The following tests should be performed on the sample to establish the re-
quirements for gravity separation. The procedure is as follows and an
example appears in Figure 60.
Equipment Required: I. I liter or similar graduated
cylInder.
2. Raw wastewater.
3. Stop watch or wrist watch with
second hand.
k. Ruler.
5. Chemicals
6. Pipette.
7- Pipette Bulb.
8. 100 ml graduated cylinders.
Procedure for Separation Tests: I. Place graduate on a level surface.
2. Fill with 1,000 mis of sample.
3. Record position of the solids/
liquid interface (POI) with time
(see example data).
Calculations for Separation
Tests:
Procedure for Chemical Settling
Tests:
I. Pfot the interface versus time.
2. Establish the settling (or rise)
rate from straight line portion
of graph.
3. If settling rate (or rise rate)
(from 2) is less than .031-0.153
mpm(0.l to 0.5 fpm)do
-------
Volume of Sol ids
Time (min) Phase (ml) POI (m)
0
1
2
3
5
8
10
12
15
20
25
30
1000
950
900
850
750
600
500
400
200
175
175
175
0.349
0.332
0.31**
0.299
0.264
0.212
0.178
0.143
0.073
0.065
0.065
0.065
Plot the data using time as the X-coordinate and POI
as the y-coordinate.
The slope of the straight line portion of the curve
represents the settling rate of the solids in meters
per minute
PC I
(m)
Time (min)
Height of Cylinder
Intersection of Straight Line with Abscissa
Figure 60. Example of settling test graphs.
286
-------
Calculations for Chemical
Settling Tests:
2.
3.
5.
6.
7.
8.
I.
2.
Choose appropriate chemicals
from Table 27.
Add in dosages at the endpoints
of the range and various Intervals.
Mix by covering the cylinder and
inverting 3-4 times.
Flocculate by holding cylinder
at the top and rotating for
1-2 minutes.
Observe floe formation and
noticable settling.
Explanation;
Large floe or
small floe which
settles well is
desirable/the
clarity of the
liquid portion
around the floe
is also Indica-
tive of the
effectiveness.
If dosage In-
creases do not
aid or improve
settling, another
chemical or a
combination of
chemicals should
be utilized.
Choose chemical and proper dosage/
scale up to 1,000 ml graduate size.
Repeat settling test but add
chemicals/mix and flocculate and
then record settling rate (steps
3-6).
Calculate the amount of chemical
required per gallon of wastewater
(see Section 7.8)
Determine settling or rise rate
as for non-chemical settling rate
(i.e., graph + slope method).
287
-------
Evaluation of Data from
Settt!ig Tests: I. Calculate detention time as
follows:
detention time »
process ht. of tank x (2 to 3)
settling (or rise) rate
2. Place new sample in 1,000 ml
graduate, treat with established
chemical dosage (if any) settle
for calculated detention time,
measure sludge height (as com-
pared to height of cylinder be-
tween 0 ml - 1,000 ml) and
sludge volume.
6.5.3 Evaluating Needed Pretreatment Schemes
There are various options available for pretreatlng the raw process flow.
When the sedimentation tank is considered optional in the flow schemes
listed In Table 22, or even when it is required, the pretreatment system
must be evaluated. The following possible systems are described and
numerically coded below for specification in the following criteria evalua-
tions.
0. No Pretreatment - Pumpage directly from the water.
I. Equalization tank only - This tank is used to simplify pumping
from the source to the next unit process and is needed so syn-
cronization or smooth operation of pumps Is not required.
2. Gravity Separation tank only - This tank is used to provide
floating or settling solids removal. A bank of systems is
necessary to provide flow through the process even during an
hour's detention time.
3« Presettler and Sedimentation Tank - This system provides con-
tinuous solids removal in the presettler followed by sedimenta-
tion, often chemically treated.
Various methods can be used to establish the type of pretreatment required.
When answering the following questions, the final choice of pretreatment
is based on the highest number Indicated by the criteria:
Criteria I: Type of pumping system: a. centrifugal 0
b. reciprocating I
288
-------
Criteria 2: Type of operation:
Criteria 3= Next process in
Sequence:
Criteria 4: Settling Rates
(from Bench Tests)
Criteria S' Sludge Volume
Criteria 6: Flow patterns in
System:
a. suction point in water 0
column only.
b. total dewatering of area. 2
c. surface skimming 2
d. bottom skimming, dredging 3
a. filtration 2
b. precipitation 2
c. neutralization I
d. oxidation/reduction I
a. greater than 1.53 mpm 3
(5 fpm)
b. 0.153-1.53 mpm (0.5-5 2
fpm)
c. less than 0.153 mpm 0
(0.5 fpm)
a. 3% or more 3
b. 0.5 - 3% 2
c. 0.5* i
a. steady flow/continuous 0
b. steady flow/intermittent I
I
c. fluctuating flow/con-
tinuous.
d. fluctuating flow/ I
intermittent
In summary the following criteria justify the use of a presettler:
I. The raw flow is the product of a dredging operation. The high sur-
face area of sedimentation tanks makes them difficult to desludge.
289
-------
2. A reciprocating pump, such as a diaphragm pump, will transport raw
flow to the sedimentation tank (especially tanks made from commer-
cial swimming pools with thin plastic liners).
3. The raw flow pattern Is intermittent or sporadic in nature.
4. The settling rate is greater than 1.53 mpm (5 fpm) or the sludge
volume Is greater than 3% of the Influent volume.
A sedimentation tank is needed when:
I. It Is to precede a filtration process - since sedimentation will
allow removal of solids prior to filtration and permit an acceptable
forward flow duration before backwash is necessary.
2. A settling rate of 0.153-1.53 mpm (0.5-5 fpm) and a sludge volume
of less than 3% of the Influent is available.
Explanation; As a pretreatment device for dual media filtra-
tion, the sedimentation tank plays a crucial
part in establishing a reasonably long interval
between backflushes (a maximum of one backflush
per day is desirable).
6.5.4 Design Considerations
If gravity separation is to be accomplished without chemical precipitation,
proceed with the following design considerations under either;
A. Sedimentation, or
B. Flotation
If chemical precipitation is required turn to Section 6.6.9.
A. Design Considerations for Sedimentation
I. Apply data from settling tests to establish a detention time.
Detention time » process height , (safety
__ v "I
settling rate J factor) * floe + mix time.
Example;
Assume; process height - 0.91 m (3 ft.)
settling rate » 0.061 mpm (2 fpm)
floe time « 10 mln.
mix time » 2 min.
290
-------
Total Det.
Time « *»5 i 10 + 2
« 57 min.
Explanation: The minimum process height Is 3 feet
and the large safety factor over-
comes scaleup problem. If floccula-
tion and mixing times are needed as
shown in Table 27, add these to the
detention time.
2. Choose a tank type (Section 7.3) using the following criteria:
a. The shallower the tank, the shorter the detention time
required for sedimentation. The minimum process depth
should be 0.9 m (3 feet) and the minimum freeboard about
15 cm (6 In.). However, shallower tanks must be desludged
more often.
b. Choose a suitable desludging technique before finalizing
tank selection:
Flat bottom tanks - Tanks up to about 8 m (26 ft) In
diameter can usually be desludged with a swimming
pool cleaner with its flexible hose connected to a
solids handling pump. The swimming pool cleaner in-
corporates a suction fitting mounted on rollers to
allow movement along the tank bottom without tearing
liners. Technique is limited to stlty muds and other
loosely packed sediments. Exclusions are gravel,
fibrous debris, leaves, twigs, and grass which would
justify the use of a presettler and/or screen chamber.
A swimming pool cleaning device is also well suited
for removing floating material.
Slopesidedtanks - In ground tanks can be excavated to
provide sloped sides leading to a single low point. A
hose suction can be located at the low point and used
as a stationary desludging point. Long-handled push
devices can be used to move the sediment toward the
suction point. Screening can be fitted around the
hose outlet for protection from fouling where necessary.
291
-------
TABLE 27. TREATMENT CHEMICAL INFORMATION
Chemical Use
Ferric Chloride organic
i norganic
Alum organic
i norganic
Poly-electrolytes inorganic
Cat Ionic
ho
>Xl
M Anionlc
Nonanionic
Alum & Poly inorganic/
organ ics to
increase
strength of
floe
Ferric chloride inorganic/
& Poly organics to
increase
clar i ty
Strength Common dosage, mg/1
25-100 mg/ml ^1000 mg/£> 50-500 mg/£
solution + lime to pH 6 or
or greater
25-50 mg/ml 1000 mg/£,SS 100-1000
solution mg/H + CaO or NaOH to
pH 6.5 to 7-5
0.5-1*
solut tons :
SS <1000 mg/2. 1-10 mg/Jl
SS >1000 " 1-300 "
SS <1000 " 0.5-5 "
SS >1000 " 1-100 "
SS <1000 " 0.5-5 "
SS >1000 " 1-100 "
Alum 100-1000 mg/X.
Poly 1-10 mg/X.
Ferric 50-500 mg/X,
Poly 1-10 mg/X,
Field mix time3
complete
dispersal of
chemical (approx.
2-5 min) .
Complete
dispersal of
chemical (approx.
2-5 min).
complete disper-
sal of chemical :
(approx 1 -2 min) .
complete d isper-
sal of chemical
(approx 1 -2 mtn)
then poly & mix
about 1 min.
Complete disper-
sal of ferric
(approx 1 -2 mtn)
then add poly &
mix about 1 min.
Field
floe time
5-15 min
5-15 min
5-10 min
2-5 min
5-10 min
2-5 min
5-10 mln
a. If required flocculation time exceeds the maximum time, try a higher chemical dosage.
-------
c. Calculate the tank volume, Vn according to the formulae
presented In Figure 73-
Example; Tank 6.1 m (201) diameter pool (Tank type A)
5-8 m (19') effective diameter
0.9 m ( J1) process height
VR - .78 D2 x Hp - .78 (5.8m)2 x 0.9m - 23.6m3
or, expressed in English units
Vn - 0.78 (19ft)2 x 3 - 842.5ft3 x 7.^8 gal =» 6360 gal.
3* Calculate Fill and Draw Times
'fill - Vaw Vn a
- -
pump rate p
Example :
Assume; Qp - 0.66cum/mtn (175 gpm)
Explanation: The process flow rate has been established by evaluat-
ing limiting factors (See section 5-1*).
*». Calculate total time of tank use per batch.
TT » total time = 2t(fm) + td (detention time)
Ex.amPle.: TT - 2 (35-7) min + 57 min
tfiH ° tdraw - 30.3cum = ^^
oTSTcum/m i n
- I28.l» min
= 130 min
Explanation; The total time needed for operation is the fill time
plus draw time plus detention time. As the tank fills
with sludge, the total time will decrease, however,
this calculation provides a safety factor. Higher
pump rates for fill and draw will also provide a
safety factor-
5. Establish frequency of desludging.
Time between desludging = 0.25 x Hp x _ T _
accumulation of sludge
batch
293
-------
Explanation: Sludge can accumulate to I A of the process
height before des Judging so the difficult de-
sludging operation is less frequent.
Accumulation of sludge height of sludge In test . ,„._,.
- - L " height of liquid in test x prOCCSS helght
Examp 1 e
Assume: I.I cm of sludge in test
36. J« cm of liquid in test
0.91m (3 ft) process height
accumulation of sludge_ *» I.I x (C.910)m
batch 36tV
» 0.028m/batch
time between desludging « 0.25 x .9\m x 130 in In/batch
0.028m/batch
» 1056 min.
» 1 8 hours
Therefore desludging can occur once per day or once every 1 6 hours
because the operations have a scheduled down time then.
6. Calculate the reduction in tank volume caused by sludge accumula-
tion.
amount of sludge accumulation « amount of sludge x batches
between desludgings batch before des I udg i ng
batches before desludging - time between desludqinq
time per batch
Example:
amount of sludge B .028m x 16 hr/between desludging x 60 m In/hour
batch 130 min/batch
Calculate new effective depth
Effective depth = process height - amount of sludge accumulated
between desludgings.
Examp I e :
Assume: process height a 0.91m
height of sludge B 0.207m
effective depth - 0.91m - 0.20?m = 0.703m
-------
Explanation;
Explanation:
Based on the assumption that sludge is accumulat-
ing at a uniform rate during the cycle, the
average amount of sludge in the tank through-
out the cycle would be one-half of the total
amount of sludge collected, making the above
calculated effective depth too low by one-half
of the final sludge height. However, the ineffi-
ciency of the drawoff operation only allows
the tank to be drawn down to twice the height
of the sludge blanket which substantiates the
above equation.
The effective volume can then be used in future
calculating.
New effective volume:
Vn eff
irD2
*TJ
x eff depth
Examp I e ;
Assume ; 5.8m - Tank diameter
eff depth » 0.703m
Vn eff « 18.6 cum
7. Calculate Process Volume Required
Vp - Qp (TT)
Examp 1 e ;
Ass uine ; Oj> • 0.66 cum/mi n
TT • 130 ml n.
Vp « 0.66 cum/mln x 130 min.
» 85.8 cum
Explanation: Qp is set by systems approach.
in Step '».
8. Calculate number of tanks needed.
TT is calculated
n - Vp
Examp 1 e ;
n
n
Vp =
Vn~eff.
k. 66 tanks
5 tanks
85 • 8 cum
1 8. A cum/ tank
295
-------
9- Calculate the sludge volume accumulated per day: sludge volume/day
=» height of sludge x 2 x number of desludges x TrD2
day ~T~
= 0.20m x 2 x I x 3.l*» x (5.8)2m
= 10.9 cum
day
10. Calculate number of sludge tanks needed:
n . • s1udge vo1ume/day
9 volume of I tank
Example; volume of I tank - 23.6 cum
"si « 10.5 cum/day «... . .
23.6 cum/tank °'5 : need one tank
B. Design Considerations for Flotation
I. Apply data from the batch tests to establish a detention time.
Detention time * process height x 3 (safety factor) + floe time
rise rate + mix-time
Example: process height » 1.22m (k ft)
rise rate ° 0.061 mpm
no chemicals
added
Detention time » I^22m x 3 - 60 min
0.061mpm
2. Choose a tank type (Section 7.3)
Remember; The system must be skimmed between each operation so the
tank geometry should be chosen to simplify this process
(Tank diameter should be 7-63m (25') maximum).
Examp1e; 5.^9 (18') diameter pool
5.19 (I71) effective diameter
1.22 ( V) process height
Vn - 0.78xD2 x hp • 0.78 (5.19m)2 x 1.22m «• 25.^3 cum
Vn (gal) - 0.78 x (17ft)2 x M x 7.1«8 gal)
« 67k gal.
296
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3- Calculate the fill and draw time.
*f i 11 « tdraw - Vn - Vn.
pump rate Qp
Exampjle: 0.568 cum/min
Assume; Qp ((50 gpm)
tfill • 'draw - 25.63
0.568 cum/min
• 1*5 min.
k. Assume a time needed for skimming the tank.
Example;
Surface area » 0.78D
= 2lm2 or 22§ ft2
Time = 1.07 min/m2 X 21m2
- 22.5 min
Explanation; Assume a skim time of I.07 min
~~i?
of surface area. However, some skimming can
be done during the operation (i.e., detention time)
and the draw time and this will reduce the time.
5. Calculate total time of tank use per batch.
TT = total time « 2(t^.,.) + td (detention time) + tg (skim time)
Example: T - 60 * (^5)2 + 23
- 173 min.
Explanation^ The maximum time for these operations is shown.
However, the total time may be reduced if some of
the skimming could be done at the same time the
tank is drawn down.
6. Calculate the reduction in tank volume caused by settled sludge
accumulation.
a. Calculate amount of sludge accumulated per batch.
Assume: from settling tests the sludge = 0*3% of total height
sludge accumulation » sjudge accumulation x Hp
!00
297
-------
Example; • 0.3 x .22m f 0.0037m/batch
100
b. Amount of sludge accumulated per day
Assume; 16 hours of operation
amount of sIudge a amount of_sIudge x batches
day batch day
batches per day • tjme of operation per day
TT
Example;
amount of sludge « 0.0037m/batch x 16 hour/day x 60 mtn/hr » 0_.02lm
day 173 mln/batch
C. New effective depth
Hp - sludge accumulated • effective depth
day
d. New effective volume
Vn - 0.78 x (5.l9m)2x I.199m
• 25.19 cum
Vn (gal) - 0.78 (I7)2 ft2 x 3.93 ft X .48 gal/ft3 - 6627 ga.
Explanation; The skimming volume is not included since the tank
is skimmed each time and the volume is not affected.
7. Calculate the process volume required.
Vp - Qp (TT)
Example; - 0.568 cum/min x 173 mln
» 98.3 cum
G. Calculate the number of tanks needed:
n - Vp
Vn eTf
Exampjje; n » 98.3 cum _ 25950 gal
25.19 cum/tank = 6627 gal/tank
n = 3.9 = 4 tanks
298
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9. Calculate sludge volume and tank requirements as shown In steps
A-9 and A-10.
6.5'5 Construction of Gravity Separation Tanks and Presettlers
If gravity separation Is to be accomplished without chemical precipitation,
proceed with the following construction steps under either;
A. Sedimentation, or
B. Flotation
If chemical precipitation Is required turn to Section 6.6.9. Presettlers
are described under C in this section.
A. Construction of Sedimentation Tanks - Tank sizing has already
occurred as part of the design process in Section 6.5.4. The re*
malnlng construction steps Involve tank Installation, Inlet velocity
head dissipation and supernatant drawoff (see Figure 61).
I. Tank installation - Small areas where the tank bottom Is
flat are required at the inlet and outlet. This Is no
problem when using a flat bottomed tank but must be
considered during excavation for sloped side, In ground
tanks. The tank liner at those spots should be protected
with a rubber sheet.
2. Obtain or construct an inlet well according to the following
guldelines:
a. The configuration of the tank is not important pro-
vided that it be sturdy and have a level top edge.
b. Height: 3/4 process water height.
c. Total length of top edge - 0.336 cm/lpm (1/2 in. per
gpm) (if 55 gallon drums are used, Figure 0.373 cum/mln
(1,000 gpm) per drum. Multiple drums can be used with
a flow splitter. See Section 7.4.2.2.
d. Whenever possible, employ a non-removable section of
Inlet hose which can be adequately supported. Ex-
tend the hose about a quarter of the way down into
the tank.
e. Ballast the tank with at least 45.5 kg (100 Ibs) If
possible.
Explantlon; When the inlet pump is shut off, the
welt will syphon back to the level
of the hose end. The buoyancy force
299
-------
HOSE
SUPPORT
INLET HOSE
INLET WELL
BALLAST
SLUDGE
BAFFLE
RUBBER SHEET TO PROTECT THIN PLASTIC LINERS
OUTLET
HOSE
RUBBER SHEET
Figure 61. Batch sedimentation tank schematic
300
-------
could cause the well to tip over.
Remedies are to shorten the well or
not extend the hose down as far.
3. Construct a sludge baffle according to the following guidelines
(see Figure 61).
a. Materials heavier than water or ballasted.
b. Height - approx. 1/2 process height.
c. Length to form a semicircle around the drawoff point, 180°
from the Inlet.
CAUTION; The baffle should not be constructed as a dam
and therefore suitable gaps should be present
to allow the supernatant to flow easily around
the baffle during drawoff.
-------
Option I - Features: Continuously Operated Swirl Tank (Figure 63)
I. Velocity is dissipated through a horizontal flow pattern
which causes the tank contents to swirl.
2. The incoming fluid travels around the complete periphery
of the tank before being discharged.
3. Sequential screens from coarse to fine can separate suspended
and floating materials from the swirling fluid.
k. Oesludging and skimming can be performed continuously.
6.5.6 Operational and Maintenance Steps
A. Sedimentation
I. Fill the tank to the desired freeboard height.
2. Allow the contents to settle for a specified detention time.
3* Draw off the supernatant to the point where solids are at
the point of flowing around the outlet baffle.
Oesludging
I. Following the last supernatant drawoff operation draw down
the entire contents of the tank Keep the suction fitting or
hose end submerged at all times in the mud.
Explanation: A certain minimum amount of water is
necessary to effectively pump solids.
Keeping the suction head in the mud will
retain the necessary water in the tank.
Water can be replenished to facilitate
solids removal as necessary.
2. Reconcentration of Settled Sludges - Further solids separa-
tion will occur In the sludge storage tank and so superna-
tent drawoff can again be performed. Chemical precipitation
as described in Section 6.6.9 can also be used to increase
the separation process.
B. Flotation
I. Fill the tank to the desired freeboard height.
2. Allow the suspended material to float to the surface for a
specified detention time. Draw off the underflow, taking
precautions not to draw in settled sludges. Draw down
can probably be started during the latter stages of skimming.
302
-------
OUTLET
INLET
SCREEN
ELEVATION
VIEW
PLAN VIEW
Figure 63. Continuous operated swirl tank presettler,
303
-------
DesJudging
I. Desludge the tank during shutdown times as required.
2. Reconcentration of flotated and settled wastes can be performed
provided the wastes are kept separated.
3. Skim tank carefully taking care to remove as little water as
possible.
6.5.7 Troubleshooting
A. Sedimentation
No settling or poor settling I. Increase settling time.
2. Repeat bench testing and revise
system to include chemical
addition if necessary.
Too much sludge
B. Flotation
No effective flotation
I. Add necessary presettlers.
I. Increase detention time.
2. Repeat bench testing and re-
vise system to include
chemical addition If necessary.
6.6 CHEMICAL REACTIONS
6.6.I General
There are three types of chemical reactions being considered In this chapter.
Each of these are used to treat various chemicals as specified in Chapter k.
In general, the wastewater is pumped into a tank, the treatment chemical or
chemicals added to a predetermined endpoint, the system allowed to react and
then the treated water is removed. The three types of reactions considered
are neutralization, precipitation and oxidation/reduction.
To determine the amount of chemicals needed, bench testing operations are
necessary. These Involve small scale chemical addition to a sample of the
actual wastewater. The volume of chemical needed to treat the entire spill
and other operating parameters can then be established. After the chemical
requirements are established, the process tankage required is calculated
using procedures similar to those for gravity sedimentation. However, neu-
tralization and oxidation/reduction reactions do not produce significant
amounts of sludge and therefore, are easier to handle.
30^
-------
This section has been split into sub-sections to deal separately with the
different types of chemical reactions up to and including the sub-section
on design considerations. However, the construction details and operation
and maintenance procedures have been combined because of the similarities
In all of the chemical reaction procedures. Information on chemical in-
jection, mixing and flocculation procedures have also been presented there.
6.6.2 Process Description; Neutralization
Neutralization is a process in which hydroxyl or hydrogen ions are added
to a solution to produce an approximately equal concentration or a pH of
7. This process is used to reduce the acidic character of a spilled
chemical by addition of caustic soda (NaOH), lime (CaO) or slaked lime
(Ca(OH)2) or soda ash (^CO^). Alkaline wastewaters (pH>9) are neutralized
by the addition of hydrochloric acid (HCI), sulfurlc acid (H2SOi,) and
acetic acid (HCH^COOH).
The specific reagents to be added are indicated on the actual flow scheme
in Chapter A. Strongly basic, NaOH, or strongly acidic, H2SO. and HCI,
chemicals must be added very carefully to avoid creating a violent reac-
tion. Complete mixing of the contents is especially important |o avoid
pockets of strong chemicals in the tank. The other reagents are considered
weaker acids (acetic) and bases, (lime and sodium carbonate (soda ash)).
In some schemes, acids used may be interchangeable with others and the
choice is established by acceptable an ion concentrations in the discharge.
Any discharge restrictions for chloride, sulfate, or acetate Ions should
be established before the reagents are used. In general, strong reagents
react faster than others. Lime has a relatively slow reaction rate and
should be slaked with water before use. Even after slaking, the reaction
time should be extended.
To establish the amount of neutralizing chemical needed, a bench scale test
is performed. The endpoint of the reaction is a change in the pH to the
desired or required level, generally pH 6-9. The diluted chemicals are
added to a sample of the actual wastewater and then the required amounts are
scaled up to allow both ordering of chemicals and treatment of the Indivi-
dual batches.
Generally, a 10 minute complete mix has been found to be satisfactory In
field operation, however, addition of lime may require 15-30 minutes to
stabilize and this extra time must be allowed.
6J6.3 Bench Testing Procedure -Neutralization
Equipment needed: I. Beaker (preferable 500-1,000 ml).
2. Burette or graduated pipette.
3. Burette stand or pipette bulb.
k. pH meter or pH paper.
5. Mixing apparatus.
6. Graduated cylinder = 1/2 volume beaker.
305
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Chemicals needed:
I. Acidic wastewater
Procedure:
Calculations for
Neutralization Test:
a. slaked lime slurry - 100 mg/ml as CaO
b. 100 mg/ml NaOH (sodium hydroxide).
c. 100 mg/ml Na£CO^ (sodium carbonate)
2. Alkaline wastewater
a. 100 mg/ml HCI
b. 50 mg/ml HaSOl,
c. 100 mg/ml HC^COOH
I. Place known volume of wastewater into a beaker
two times Its size.
2. Mix and record initial pH.
3. Add neutralizing chemical in Increments and
record volume added and pH after equilibrium
has been reqched (lime requires a longer time
to reach equilibrium).
4. Continue adding neutralizing chemicals to
reach pH k or pH 10.
5. Plot neutralization curve, pH versus amount of
chemical/1 Iter of wastewater.
6. Choose desired pH, (usually 7) and corresponding
dosage.
7. Repeat steps I and 2 and then add the amount
of chemical required to achieve desired pH
(usually 7).
8. Record time required to achieve final pH, note
volume of any accumulated sludge.
I. Calculate the amount of chemical required per
gallon of wastewater (see Section 7.8) and for
entire spill.
2. Estimate the amount of time required per
batch (see Table 28).
3. Calculate volumes of sludge produced per
gallon of wastewater (if any).
Volume of sludge « volume
^
volume test sample
wastewater to be treated.
306
x volume of
-------
TABLE 28. CHEMICAL REACTION OPERATING PARAMETERS
Process
Mixing
Type
Time
Endpoint
Chemicals
Chemical
Sedimentation
Neutralizat ion
Rapid
Flocculat ion
None
Rapid
Preci pi tat ion
Rapid
Flocculat ion
None
Oxi dation
Chlorination
Aeration
Reduction
Rapid
Ai r mix
Rapid
1-5 min
5-15 min
30-60 min
depends on rate
and process height
10-30 min
Use 30 min for 1ime
addi tion
1-5 min
5-10 min
30-60 min
depends on rate and
process height
10-30 min
depends on test
10-30 min
Clarified water
and good
settling
Add to pH 7, use
pH paper or meter
to check
Varies to a pH
or unti1 res idual
of reactant or
until clarified
To a HOC1 residual
of 1 mg/1
D.O. measure to
70% of saturation
or other
Large ORP change/
Cr+6 — Cr+3 is
yellow to green
HOC! reduction, no
Chlorine residual
Ferric Chloride
Aluminum Sulfate
Polyelectrolytes
Calcium Hydroxide,
Calcium Oxide, Sodium
Hydroxide, Sodium
Carbonate, Sulfuric
Acid, Acetic Acid,
Hydrochloric Acid
Calcium Hydroxide,
Sodium Hydroxide,
Sodium Carbonate,
Sodium Biocarbonate,
Sodium Sulfate, Sodium
Sulfide, Potassium
Chloride
Sodium Hypochlorite
Air
Sodium Bisulfite,
Sodium Sulfide
-------
6.6.4 Process Description; Precipitation
Precipitation is a process which removes pollutants by reacting these materials
to form an insoluble product (51). This process results in a reaction rather
than physical adsorption and is therefore different from coagulation and
sedimentation, however, treatment construction is similar. There are a series
of steps to allow effective precipitation: I. chemical addition; 2. rapid
mix; 3. addition of coagulant; *». flocculation; 5. sedImentation}and 6. fil-
tration. However, each precipitation reaction may not require all of these
processes and secondly all of these steps except filtration can be performed
in one tank.
Precipitation is used to remove many types of metal cations and some anions
such as fluorides and sulfides. The reagents Involved in the precipitation
reactions include calcium and sodium hydroxide and sodium carbonate, bicar-
bonate, sulfate and sulfide. These chemicals are added to reach certain pH
or in some cases to a small residual of the reagent. Sulfide amount and
addition can be checked using an electrode or by reacting with zinc acetate.
The sulfide residual is present when a white precipitate appears or if zinc
acetate indicating paper changes color. However, excessive sulfide addition
must be avoided because of the strong reducing ability of this material.
The other precipitation chemicals (e.g., lime, soda ash) are added to a
specific pH, allowed to mix and then to settle. If no definitive test is
available, the addition of a reactant to a distinct floe, and then analysis
of the supernatant for the contaminant is necessary. However, the metallic
hydroxides are difficult to remove so coagulation and flocculation using
alum, ferric chloride or polymers (or a combination) may be helpful. The
procedure to establish chemical dosages of the coagulant is the same as that
outlined in the gravity sedimentation section.
The amounts of chemicals required to precipitate the entire reactant are
determined by running a bench scale test. This test is similar to the pro-
cedures outlined earlier in Section 6.5* A known volume of wastewater
sample is reacted to the endpoints specified in the treatment specifications
from section 6.5.2, The chemicals are mixed, reacted and then settled. If
necessary a coagulant is added to improve the settling. Once the test is
completed, the data is scaled up to determine the amount of chemical re-
quired. In general, 25% excess chemical should be ordered.
When operating a field unit, the tank contents should be mixed completely for
5-10 minutes (or t5~30 minutes if lime is added). If flocculation is re-
quired, a 10-15 minute flocculation at a speed just fast enough to keep the
solids suspended is required: the settling time will be equal to
[height of tank m ] , .
[settling rate m/min] x { 5)
The 2-3 is the scaleup factor for most settling operations.
308
-------
6.6.5 Bench Testing Procedures Precipitation
Equipment needed:
Chemicals needed:
Procedure:
I. Beaker (preferable 500-1500 ml).
2. Graduated cylinder ( 1/2 volume of beak-
er) .
3. Burette or graduated pipette (pipette
is better for lime addition).
k. Burette stand or pipette bulb.
5» pH meter, or pH paper, or chemical test-
ing kit, or zinc acetate paper, or zinc
acetate
6. Mixing apparatus.
7. 1,000 ml graduated cylinder.
8. Stop watch or watch with second hand.
I. lime (calcium hydroxide) Ca(OH)2>
2. Sodium hydroxide NaOH.
3. Sodium carbonate Na2CO,.
4. Sodium bicarbonate NaHCO..
5. Sodium sulfate Na-SO..
6. Sodium sulfide Na2S.
7. Coagulants
a. ferr ic chlor ide.
b. aluminum sulfate.
ck polyelectrolytes.
8. Sulfucic acid (H2SO.) may be needed.
I. Place known volume of wastewater into
beaker two times its size.
2. Mix/record initial pH.
3. Add acid to adjust pH if necessary.
309
-------
*». Add reagents (as indicated) in incre-
ments and record pH until the desired
pH level is reached while mixing for
2 minutes. If pH is not the controll-
ing factor as for sulfate:
Take samples at increments after
mixing and analyze for sulfate con-
centration using Hach kit or
spectrophotometer.
For sulfide:
Take samples at increments after
mixing and analyze for sulfide con-
centration using a S** probe or pre-
cipitation with zinc acetate (paper
or chemical).
For others:
Add chemical until a good floe is
formed.
5. Allow to settle and note the rate of
settling using a stopwatch and incre-
ments on the beaker.
6. Take sample of supernatant for analysis
of contaminant.
7. Plot pH versus volume of reagent added/
liter of waste, sulfate/sulfide resi-
dual versus volume of reagent added/
liter of waste or concentration of
contaminant versus volume of reagent
added.
8. Choose point on curve to establish
amount of reactant needed.
9. Place another wastewater sample into 1
liter and add chemical while mixing.
10. Check to insure endpoint has been
reached.
If the settling is poor, add coagu-
lants in the amounts indicated in
the previous section and establish a
new settling rate (section 6.5-2).
310
-------
12. Note sludge volume and height in the
cylinder.
Calculations from
Data: I. Scale up the results to establish the
amount of chemical required per volume
of wastewater to be treated.
2. Calculate amount of sludge expected per
volume of wastewater.
3- Calculate the amount of time needed
for entire reaction (see Table 28).
6.6.6 Process Description; Oxidation/Reduction
Oxidation/reduction involve the transfer of electrons from one
species to anogher. Oxidation involves the loss of electrons and re-
duction, the gain of electrons. In some instances these reactions can
be used to change hazardous species into less harmful forms.
Reduction: In this manual, reduction reactions are only applicable to a
small number of compounds. Sodium bisulfite has been recommended as the
reducing agent, however, other chemicals including sodium sulfite and
sodium metabisulfite can also be used. Reduction is used as a pretreat-
ment for chromate or chromyl compounds to change them to the chromic
state for precipitation. This reaction must occur at low pH, so adjustment
to pH 2-3 with acid is recommended. The endpolnt is best determined by
either a large oxidation reduction potential (ORP) change, as measured by
a platinum electrode, or removal of the chromate (e.g. Cr*") as measured
by a chemical test. A visual indication is the color change from yellow
to green and it can be used as a confirming indicator. Reduction is
also used when either sodium or calcium hypochlorite are to be removed.
The pH is reduced to three and the reducing agent can be added until an
acceptable chlorine residual is measured. Excess reducing agent can be
removed by addition of more wastewater or aeration.
To determine the amount of sodium bisulfite, or its equivalent, to order,
a small scale bench testing procedure is used. A known volume of waste-
water is placed in a beaker and the reagents are added to the endpoints
indicated in the treatment specifications. The reaction time and any
sludge volume should be noted by the OSC.
Once the amount of chemical required has been established, the chemicals
should be ordered from suppliers. In operating a large scale reduction
process, the acid should be added (75%. then in increments) and mixed
approximately one to two minutes and the pH should be determined. Then
the bisulfite can be added to the pre-established endpoint, in the same
manner, e.g., add 75% of the total and then increments until the endpoint
is reached. The tank should then be mixed for ten minutes to insure
complete reaction and then the residual rechecked for discharge.
311
-------
Oxidation; Oxidation reactions are more common than reduction and more
reagents can be used. Chlorination and aeration are two ways to oxidize
materials. Chlorination is discussed here and aeration is addressed in a
later section.
Chiorination reactions are most commonly used to oxidize cyanide to the
less toxic cyanate and then to carbon dioxide and nitrogen. These
reactions are most effective at alkaline pH so soduim hydroxide is often
added with hypochlorite. The chlorine is most safely added in the form
of liquid hypochlorite in concentrations of $%-(>% (household bleach).
On a bench scale the concentration is diluted tenfold or more. Chlorine
doses are determined by doing a bench scale test until a slight residual
of chlorine remains as measured by a test kit. Once operating in the
field, both NaOH and hypochlorite should be added at 75% of the ex-
pected volume and then in increments to the desired endpoint. The sys-
tem should then be mixed and additional 15 minutes and the residual
chlorine tested before discharge to be certain it meets acceptable limits.
6.6.7 Bench Test Procedure • Reduction
Equipment needed:
Chemicals needed:
Procedure:
I. Beaker (500-1500 ml).
2. Graduated cylinder ( 1/2 volume of
beaker).
3. Burette or graduated pipette.
k. Burette stand or pipette bulb.
5. pH paper or meter.
6. ORP meter, chemical test kit or
swimming pool test kit.
7. Mixing apparatus.
I. Sulfucic acid H2SO^.
2. Sodium bisulfite.
I. Place known volume of wastewater into
beaker two times its size.
2. Mix/record initial pH.
3. Add acid to pH 2-3.
k. Add sodium bisulfite to
a. large ORP change
b. removal of chromate (CR+6)
312
-------
5« React ten minutes.
6. Scale up to establish amounts of re-
agents needed.
6.6.8 Bench Test Procedure: Chior I nation
Equipment Required:
Chemicals needed:
Procedure:
I. Beaker (500-1500 ml).
2. Graduated cylinder ( 1/2 volume of
beaker).
3> Burette or graduated pipette.
4. Burette stand or pipette bulb.
5. pH meter or pH paper.
6. Chlorine test kit (Hach» swimming
pool).
7. Mixing apparatus.
I. Sodium hydroxide-NaOH.
2. Hypochlorite solution.
I. Place known volume of wastewater into
beaker two times its volume.
2. Mix/record initial pH.
3. Add NaOH to desired pH.
k. Add chlorine in increments mix and
check residual.
5. Stop adding chlorine when residual
appears.
6. Allow to mix five minutes, check
residual.
7- Add more chlorine if necessary to
reach a persistent residual.
8. Note any sludge produced.
9. Scale up to the amount of hypochlo-
rite required to treat entire spill.
313
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6.6.9 Design of Chemlcaj_ Reaction Processes^
I. Calculate amounts and order chemicals from the manufacturer (see
Section 7.9 for Information).
Explanation; Chemicals wISI require long delivery times and
should be ordered Immediately. If the total
amount of chemical Is not available immediately,
have a partial order shipped first.
2. Design the volume of chemical tanks needed to hold one day's supply
of chemicals.
a. Calculate volume of chemicals needed per day:
volume of feed solution « yo 1ume of feed soIut Ion
day "volume of wastewater
x volume of wastewater
day
b. Calculate size of tanks needed per day:
volume of tank « 1.2 x volume of feed solution chemicals
day
c. Determine If single or multiple feed tanks are needed.
Explanation; If large volume of chemicals are needed
daily, a smaller feed tank can be used
with a separate mixing tank. Chemicals
can be mixed in batches throughout the
day to provide a supply for the feed tank.
d. Repeat steps (a-c) for each chemical.
3. Apply data from bench tests to establish a detention time.
Explanation; Refer to Table 28 for general reaction times.
Follow calculations when settling Is necessary
Detention time » process height x 3
settling rate
Example; Refer to section 6.5.4 for an example of the calcu-
lations.
4. Choose a tank type using the following criteria (Section 7.3):
a. The shallower the tank the shorter the total time needed
-------
for settling, when necessary. Also, mixing gradients may be
more effective. All depths should be greater than 0.91m
(3 ft) with at least 0.305m (12") of freeboard.
b. Choose a des Judging technique if precipitation or chemically
treated sedimentation Is used. Refer to section 6.5.^ for
information on desludglng techniques.
5. Calculate the process volume per tank according to the formulae
presented In Figure 73-
6. Calculate fill and draw times.
'fill • 'draw Vn '
pump rate Qn
Explanation; Process flow rate has been previously established
using limiting factors design (see Section 5-1*)..
7. Calculate total time of tank use per batch.
T., » total time » 2 (tr..,) + t. (detention time)
T 1 1 1 1 d
Explanation; fill is calculated from Step 6.
8. Establish the frequency of desludglng.
time between desludglng • 0_. 25 ^x _Hp x TT _
accumulation of sludge
batch
Explanation; Desludglng must be done when the sludge accumulates
to I A of the available process height. Sludge
will accumulate considerably In the precipitation
reactions or chemically treated sedimentation.
Oxidation/reduction and neutralization reactions
should not generate much, if any, sludge. There-
fore, if sludge accumulation is negligible, Steps
8-9 can be eliminated.
Accumulation of sludge » hejght of sludge in test^ x process height
batch height of liquid in test
9. Calculate the effective tank volume. (Volume Is reduced by sludge
accumulation) .
amount of sludge accumulation a amount of sludge x _ batches
between des Judging batch before desludg-
Ing
batches between desludglng » time between desludglng
time per batch
315
-------
Calculate new effective volume
Vn eff » irfl2'x effective depth - 0.78 D2 x effective depth.
-
10. Calculate process volume required.
vp - Qp (TT)
Explanation; Q^ or system flow rate is already established.
II. Calculate number of tanks needed.
n ** Vp
Vs77
Explanation; Always round n to the higher round number.
12. Calculate the sludge volume accumulated per day.
sjudge volume^ *
day
2
(height of sludge^ x 2^x number^ of batches x 0.78 D )
per batch' "*"day
Explanation; It is assumed that the sludge Is disposed of
once per day and the tanks are cleaned for the
following day.
I3. Calculate the number of sludge tanks needed.
n . « sludge volume/day
volume of I tank
Explanations It is assumed that the sludge disposed of once
per day and the tanks are cleaned for the following
day.
14. Calculate the capacity required for each rapid mix tank.
V - 5 x " t0
VRM 5 X
Qp » process flow rate from Section S.k
Explanation; The rapid mix tank will be designed on a continuous
flowthrough basis with a detention time from 5*10
minutes. One tank will be necessary for each
process tank.
316
-------
15* Choose rapid mix tank type from Section 7.3 following these
guidelines.
I. Sturdy construction.
2. Compatible materials for chemicals being added.
3. Height to diameter ratio 0.5-1.5 if possible.
6.6.10 Construction of Chemical Reaction Processes
Two separate systems are described here to accomplish the various chemical
reaction requirements; aeration processes are discussed separately.
A. Chemical addition and mixing.
B. Chemical addition, mixing and flocculation.
A. Chemical Addition and Mixing - This option is used for the addition
and mixing of one or more chemicals in a continuous flow rapid mixing
tank followed by chemical reaction to a predetermined endpoint in a
batch operated tank. A schematic diagram of the system is shown in
Figure 6k. Construction details follow.
I. Install rapid mix tank as instructed in Section 7-3.
a. Construction of submerged jet (Figure 65) for the process
flow transfer pump (52).
Explanation: Recommended for most mixing conditions,
although the faster mixing chemicals will
be properly mixed from the normal transfer
hose discharge velocities.
Principle of operation - When a submerged jet is introduced
into a tank, the jet stream traverses a significant distance
through the water before the jet stream velocity dissipates.
The jet tends to entrain fluid, producing significant mix-
ing and the creation of a turbulent zone.
I) A nozzle can be constructed by installing a combina-
tion nipple into the hose end of transfer pumps I
and 2 and bushing It down to the desired jet diameter,
D| (see Figure 65).
Explanation; Commercially available tank educ"
tors may also be used; they have
a shroud around the nozzle to in-
crease entrainment and intensity of
the turbulence.
Jet diameter will depend on tank
configuration and detention time
317
-------
TO NEXT
PROCESS
PROCESS
FLOW
TRANSFER
PUMP #1
(FROM PRECEDING
PROCESS)
NOTE: ALL PROCESS PUMPS TO
HAVE SAME CAPACITY
1
1
1
ICAL |
ED 1
1P ~ *|
1 . tS~\ )
*. . .. /"•" — y i '
) 1} *"^^
' ... PROCESS
RAP 1 D FLOW
MIXING TRANSFER
TANK PUMP #2
RECIRCULATIO
DISCHARGE P
, S~\
Q — i
i
lh i
k
CHEMICAL
REACTION
TANK
(OPTION_Aj
N AND
UMP
CHEMICAL REACTION
MmNG_,_AND FLOCCULATICJN
(OPTION B)
CHEMICAL MIXING
AND AERATION
(OPTION C)
Figure 6k. Schematic diagrams of chemical treatment options.
318
-------
HOSE END
EFFLUENT
INFLUENT
HOSE CLAMP
,_ COMBINATION NIPPLE
| r- PIPE COUPLING
*' . j If— PIPE ADAPTER
D
HOSE CLAMPS
ENTRAINED
FLUID
Lii—
MIXING ZONE
^i 111 n • im LVM
TYPICAL JET ASSEMBLY
EVALUATION VIEW OF
JET ACTION IN TANK
TURBULENT
JET
JET SUPPORT
PUMP
INFLUENT
EFFLUENT
DISCHARGE
HOSE
SUCTION
HOSE
PLAN VIEW OF RECIRCULATION
ACTION IN TANK
Figure 65. Installation of jet mixer in rapid mix tank.
319
-------
and so It is desirable to obtain
bushings in the size range calcu-
lated below and basing the final
selection on a tHal basis (52)
to /i (lnches)
7 20
where Qp = process flow (gpm) gpm
gpm x 3.785 x I0"3 » cum.
Explanation; The above formu-
la will provide
a discharge ve-
locity range from
6.1-9.1 mps (20-
1*0 fps).
2) The jet must be adequately supported In the tank because
the reaction force from the jet will tend to push the
hose backwards.
3) When sizing the effluent pump add 21.3m (70 ft) to the
total friction head to account for the nozzle head loss.
4) Guidelines 'for placement of nozzle and suction hose*.
Orient the jet stream so that it traverses a long dis-
tance before hitting a tank wall.
Position the effluent suction hose behind the jet. Alter
the location of jet and suction as necessary to achieve
thorough turnover of the tank contents.
2. Chemical reaction tank - same as construction of sedimentation tank
3. Chemical injection - usually submerged and located in the inlet
well.
B. Chemical Addition, Mixing and Flocculation^ - This option is used for
the addition of one or more chemicals followed by flocculation and
sedimentation. A schematic diagram of the system is shown in Figure 66.
Construction details follow.
I. Rapid Mixing Tank - identical to construction option A, Steps 1-2.
2. Construction of Flocculation Tanks (Figure 66) - Tank, sizing
has already occurred as part of the design process in Section
6.5«5« The remaining construction steps Involve flocculator
construction, inlet well, and outlet baffle.
320
-------
OPTIONAL STRUCTURE, FOR STRENGTH
ROTATING ARM
j— PADDLE BRACKETS
PADDLE SLATS
PIVOT
*- Rll
INFLUENT
HOSE
HOSE SUPPORT
BALLAST
RUBBER SHEET
PIVOT PIPE
INFLUENT WELL
INFLUENT
HOSE
CLEARANCE DIAMETER
BAFFLE
EFFLUENT
HOSE
Figure 66. Construction of a mechanical flocculator.
32i
-------
The gentle rolling action necessary for flocculation requires
a minimum of fluid shear to disrupt the floe. It can be
produced with a canoe paddle in certain cases using the sedi-
mentation tank construction described in Section 6.5«5« If
possible, the construction of a flocculator as described be-
low will give much more satisfactory mechanical results.
a. Tank installation - A flat bottom tank is required.
Tank liners should be protected with rubber sheets
under the inlet well and outlet baffle. A 0.9-1.22m
(3-*» ft) clear space is needed all the way around the
tank.
b. Obtain or construct an inlet well according to the
following quidelines.
I) The configuration of the tank is not important
provided that it be sturdy (preferably steel) and
have a level top edge.
2) Total height approx: 3A process water height.
3) Total length of top edge approx 0.336m/1pm
(1/2 inch per gpm).
4) A hole must be cut to permit the installation of
the inlet hose. After insertion of the hose in-
to the hole, rags or other packing should be
used to close off the opening around the hose.
5) Install a pivot post, e.g., steel pipe, in the
tank. The pipe can be welded to the tank
bottom and supported by three bars to act as
post supports at the top.
6) Ballast the tank with heavy weights to provide
stability approx. 45.5-91 kg (100-200 Ibs) of
metal. Place ballast so as not to interfere
with free flow of inlet hose.
c. Construct the Flocculator Assembly from wood or pipe as
shown in Figure 66 according to the following guidelines.
Rotating arm - long enough so that it can be held by a
person who will walk around the tank.
Pivot - very solidly joined to rotating arm and extending
down about six inches into the pivot pipe.
322
-------
Paddle Brackets - very solidly attached to rotating arm and
mounting the paddle slats.
Note: Especially in wooden construction, it may be desirable
to use a two-arm construction which would reduce the
stress at the high stress points (shown with astericks
on Figure 66).
Paddle Slats - About four are necessary with spaces in be-
tween. Top slat should be submerged; bottom slat at a
height of one-third the process height; and inside and out-
side rotational diameters to clear the inlet well, outlet
baffle, and inlet hose.
d. Construct an outlet baffle and serrate the end of the out-
let hose as described in Section 6.5.5, Steps A, 3-k.
6..6.11 Operation and Maintenance of Chemical Reaction Processes
The mode of operation for all chemical reaction processes is batch opera-
tion with end point control. Prior to giving explicit operational in-
structions for each of the three design options described previously, the
steps necessary to produce end point control will be outlined. However,
prior to any operation, the treatment chemicals must be mixed to the
proper feed concentrations. Instructions are included in this section.
Step I: Mixing the chemicals into the desired feed concentrations.
a. Calculate the amount of water needed to dilute the concen-
trated chemical (Section 7.8.2),
b. Add water to the chemical tank and agitate using an impeller
mixer (Section 7-5).
c. Follow any specific instructions for mixing listed in the
chemical data sheets (Section 7.8.3).
d. If no special instructions are given, follow these procedures:
Soj_id_s_ - Slowly drop powder or pellets into the swirl-
ing water and mix until dissolved or in suspension. Add
more chemical until the entire amount has been added.
If a lime slurry is being prepared, continue mixing
throughout the entire operating period. Take precautions
to avoid breathing dust or directly touching the chemi-'
cals.
Uquids - Pump the concentrated liquid slowly Into the
tank using a chemical feed pump. Mix thoroughly, con-
tinue adding liquid until the entire amount has been
323
-------
added. Avoid fast addition which could result in the evolution
of large amounts of heat.
Step 2: Endpoint Measurement - In order to accurately measure the re-
action completion, the endpoint must be measured during the
actual treatment of the system. The efficiency is also a func-
tion of the effective mixture of the contents. The amount
of chemical expected to be used per batch Is first calculated,
75% is added during the influent flow and the remainder is
added in Increments to the endpoint.
a. Calculate the amount of chemical needed/batch.
volume of feed solution needed
volume of wastewater batch ~*
cone, of bench
volume of batch chemical added from bench test x scale chemical
volume of wastewater
concentration of feed solution
vo 1 ume of feed so I ut i on ...
volume of wastewater
volume of feed solution/x vpjjjme of wastewater
volume of wastewater batch
Examp 1 e: Add 25 ml of IN f^SOlj to 500 mis of sample. Volume
of process tank is 37.8 cum or (10,000) gal. Use H2SO'» a*
25?; strength or about 9 N.
-rnn- \ * rTTT = 0.0055ml 9N/ml sample
5'JO m I 9N
Metric: 0.0055 x 17-K cum = 0.201 cum of feed H2SOi(.
F.nnlish: 0.055 x 10,000 nal./batch = 55.5 qal. of feed H2SO/,
b. Determine and collect endpoint measuring apparatus.
Explanation: The endpoint device may be a pH meter,
portable chemical analysis kit, ORP
meter, zinc acetate paper or other
specific indicator. The faster the
response the better.
c. Add 75% of the calculated volume during the tank filling
operation.
324
-------
Explanation; Calculate amount to add (Step a). Use 75%
of the chemical to avoid overruning the endpofnt. After
the first batch, use 15% of the amount added to the pre-
ceding batch as the starting point. Since the strength
of the wastewater will vary throughout treatment, this
procedure provides an extra safety precaution.
Step d - Allow tank to mix.
Step e - Check endpoint of reaction at various points In the tank.
Explanation; This procedure will allow the operator to
check the thoroughness of mixing and will allow determination
of the endpoint. If the analyses give different results
at different points in the tank, then further mixing is
necessary.
Step f - Add more chemical in increments to reach the final
endpoint (again check the endpoint at various places within
the tank to insure complete mixing).
Step g - If more than one chemical is added; add the second
chemical after the first following the same procedure
except using induced recirculating mixing.
Step h - If flocculation is needed, it should begin after the
mixing is completed.
Step i - When the final point is reached, mixing can be continued
for the specific reaction period and then terminated and
pumpout commenced.
Step 3; Chemical Addition and Mixing-- All Options: At the starting
point in the process, the rapid mixing tank is about 2/3 full
and the chemical reaction tank is drawn down as far as possible
to the sludge layer.
Step a - Turn on the process flow transfer pump #1 and watch
for jet nozzle action to begin in the rapid mixing tank.
Step b - Shortly thereafter, turn on process flow transfer pump
#2 to pump at the same rate as pump #1.
Explanation: If the rapid mixing tank and the Inlet well
of the chemical reaction tank are at different levels, it
may be necessary to withdraw the suction hose of Pump #2
between operations or to put a valve in the line to prevent
syphoning. In that case, the hose must be repositioned or
the valve opened before pump #2 can be started
325
-------
Step c - As soon as the two pumps are running, turn on the
chemical feed pump at a rate calculated by the following
formula:
feed rate (gph) = volume of feed solution (gallons)
60 min x fill time (min)
hr.
gph x 3.78'' = liters per hour
Caution: Do not fill the chemical reaction tank above the
0.305m (12 inch) freeboard height to provide a buffer zone
to dilute the batch in the case where chemical reaction is
carried out past the endpoint.
Step d - Turn off the chemical feed pump and process flow trans-
fer pump #1 and immediately turn on the reelrculation pump.
Step e - Through the process of monitoring and adding Increments
of chemicals, achieve endpoint conditions for chemical #1.
Leave the recirculation pump and process flow transfer pump
#2 running during the entire procedure.
Step f - If more chemicals are to be added, recalculate a new
feed rate from the equation In Step 3.
Step g - Add this amount of chemical, monitor, and then achieve
end point conditions as described in Step 5.
Step h - Further Process Steps - After chemical treatment is
complete, the following processes may be performed before
discharge of the reaction tank contents:
a. Gravity separation - operational procedures in Section 6.5.6
b. Flocculation and aeration - operation procedures
described below.
Step I - Discharge the chemical reaction tank contents to the
next process using the discharge pump.
Explanat ion: If the recirculation hose is used for discharge
it will be necessary to remove the jet. It would be better
to use a separate hose for discharge.
Flocculation - Operational Steps
Step a - with the rec1rculation pump off, the flocculator arm
is moved through complete cycles around the tank to cause
a gentle stirring action. If the tank contents begin to
speed up in the direction of rotation, the rotation direction
can be reversed to achieve more efficient mixing.
326
-------
Step b - Continue flocculation until visual observations indicates
that a good floe has formed (usually 10-15 minutes at longest).
Step c - Refer to sedimentation operational steps. Section 6.5.6
6^.6.12 Chemical Reaction Troub 1 eshootin£
The most common problem would be that the endpoint is overshot. This will
most likely occur at the beginning of operation before the kinetics of the
reaction are familiar to the operators. When this situation occurs, the
following procedure can be used.
I. Take a sample of the overtreated water.
2. Back titrate to the endpoint using contaminated water.
3. Note the volume of wastewater needed to reach the desired endpoint.
k. Scale up the results to determine the increased volume of waste-
water to be added using the following formula.
amount of_ _w_a_s_tewate r t o re a c h en d pp ? n t vo 1 ume of wa s tewa te r
amount of overtreated water x in process tank
= volume of wastewater to be added to process tank
5. Extra freeboard 15cm (6") has been provided in the design to allow
the additional wastewater to be pumped into the tank.
Other possible problems involved in chemical reactions include:
I. Concentration gradients in tank: Check jet mixing systems to be
sure they are operating properly.
2. Incomplete chemical reactions:
after addition of entire
chemical amount:
6.6.13 Processjescri p t i on: Ae r a t1 on
Repeat bench tests and recal-
culate required volumes. Also,
if lime is used, allow system to
react longer since the rate of
reaction is slow.
Aeration is another method for oxidation. Air can be used as an oxidizing
agent which is more available but not as strong as chlorine or chlorine
compounds. In general, air is introduced into the tank at the bottom and the
air bubbles rise to the surface. As they travel
the oxygen in the air is transferred through the
where it can react with the hazardous compound.
only valuable for easily oxidized materials such
wise, lengthy reaction times would be necessary.
through the water column,
bubble and into the water
However, this technique is
as ferrous iron. Other-
327
-------
Aeration can also be used as a mixing technique, however, the necessity
of placing manifolds near or on the tank bottom may preclude this method
when sludge is accumulated. Another problem with using aeration for
mixing occurs if the sludge layer is disturbed or if a reduction reaction
is desired (the oxygen will be reduced before the hazardous compound).
Therefore, aeration has only limited application as a mixing technique.
When it is to be used, (e.g. for a neutralization system) the construction
techniques will be the same as those applied in this section. Rates of
aeration reactions are difficult to predict because a myriad of factors
affect them. Among the variables which influence aeration rate are the
following: manifold efficiency, blower efficiency, oxygen transfer rate,
impurities in the wastewater, tank depth, temperature, humidity, etc.
Therefore, a bench testing procedure is only used to establish a reaction
endpoint and the feasibility of aeration with respect to time. The
dissolved oxygen versus time can then ^e established by aerating a sample
until it reaches the saturation point. From this data, an endpoint
dissolved oxygen value can be chosen based on the desired efficiency of
the reaction. Generally, a level of 70% of saturation can be considered
the reaction endpoint. If the aeration reaction has required excessive
amounts of time to reach completion, stronger oxidation may be needed.
After the feasibility and the endpoint dissolved oxygen level have been estab-
lished, one full sized reaction tank can be constructed. This procedure
would allow the determination of the actual amount of time needed for field
reaction. Then calculations regarding the number of tanks needed for
field use can be made.
6.6. 1
l*t Testing Procedure:
Equipment needed : 1 .
2.
3-
4.
Aeration
* 5 gal
Diffuse
Air sou
Di ssol v
Chemi ca1s:
Procedure:
5-
6.
7.
8.
pa! 1
stone
ce
:d Oxygen Probe
or Burette/Burette stand/pipette/beaker/
500 ml graduated cylinder
Stop watch
Thermometer
Barometer
Large graduated cylinder
Reagents for Winkler Titration*
1.
2.
3-
k.
5.
Place known volume of wastewater into pail
(* 3A full)
Measure initial D.O.
Place diffuser stone in bottom and begin
air f1ow
Measure D.O. at appropriate increments
(varies from 30 sec - 15 min)
Keep measuring D.O. until saturation, i.e.
no change in D.O. level
328
-------
Calculation Procedure:
I. Plot the DO value versus time of aeration.
2. Choose a suitable endpoint DO valve
(usually 70% of saturation)
6.6.15 Design of Aeration System (s_ee_References 53-56)
The following design steps are necessary when designing a submerged header
with orifices used in conjunction with an air compressor or blower.
Step I - Choose an available tank from Section 7-3 according to the following
guide!ines.
a. Use a flat bottom Type A tank, preferably I.57-1.63m (62-6A in.)
total height. Freeboard height should be 0.305m (12 inches)
with a process height of I.27-1.32m (50-52 inches).
b. Select a tank with a durable liner or else place a protective
sheet within tank with thin plastic liners.
Step 2 - Determine the blower horsepower as a function of process volume,
V , using Figure 67.
Explanation^ The graph in Figure 67 was developed through use of
the mixing formula:
y Vp
V/here P = mixing power, hp
G = velocity gradient, sec
2
y = dynamic viscosity of fluid, Ib-sec/ft
Vp =• process volume in ft
Because of the wide range of variables affecting this process, the
use of the formula in preparing Figure 67 is based on the following
assumptions:
G = AOO, which is the flash mixing point (high rate mixing).
This was used as a safety factor to be sure the blower is
not undersized. In the actual case a lower velocity
gradient will probably be sufficient.
y = based on water only, more viscous substances would ele-
vate this number and raise the pressure.
However, blowers may not be readily available and a compressor may
have to be substituted even though it is not well suited for this
329
-------
METRIC CONVERSIONS
gal. x 3.785 x I0"3 - liters
hp x 1.014 - hp (metric)
- 32) 5/9 - °C
WATER TEMPERATURE
18,000
14,000
o
"n
uT 10,000
=3
O
| 6,000
2,000
I I
6 10 14
BLOWER HORSEPOWER (BRAKE)
\ \
20
Figure 67. Blower size as a function of
process volume for an aeration tank
330
-------
application. The most readily available compressors will need a
line regulator to reduce the pressure. Figure 67 does not apply to
these high pressure compressors and the manufacturer should be
consulted in the proper sizing for the application.
Example: A flat bottom tank with a process volume of 9.600 gallons
is to be aerated. The water temperature will be around 60°F .
From Figure 67 the required blower brake horsepower is 8.8 bhp.
gal. x 3.78 x 10 = cum
hp x 1.014 = hp (metric)
(°F - 32) x 5/9 = °C
Step 3 ~ Choose an available blower to provide the mixing horsepower at 5 psi
of pressure.
Explanation: The low pressure nature of aeration make low pressure
blowers, such as the positive displacement blower, the most suitable
for this application. The major pressure losses which make up the
.34 atm (5 psi) differential pressure are the following conversions:
(psi x.0868 = atm).
I. Water head = the height of the water above the orifices. e«a..
36 inches x j_J«J_ = 1-3 pst.
27.7 in
2. Orifice loss - 0.5 to 2 psi through the potential flow range,
Q (CFM) of aeration. (CFM x O.A7=Hters per sec).
3. Line losses = valves, elbows, restrictions, etc., assumed to be
less than I psi.
k. Safety factor = .7 to 2.2 psi to account for some of the varia-
tion which can result from temperature and viscosity changes,
water height change, some plugging, etc.
Example: (same example as Step 2) A local supplier of positive
displacement blowers has a blower that is rated from 2-12 psi and
has the following ratings at 4 and 6 psi.
The following conversions are appropriate:
CFM x .^72 = liters per sec.
psi x .068 = atm.
hp x I.014 = hp (metric)
331
-------
Air flow (CFH) Brake horsepower (BMP) Motor size (HP)
4 psi
211
350
554
731
1,106
6_psl_
227
394
536
694
1,041
4 psi
5.3
8.8
16.5
17.9
27-2
*-$*
13.9
21.9
25.6
37-1
4 psi
7.5
10
20
20
30
6 psi
" 10
15
25
30
40
It is necessary to interpolate this data. We are looking for a
bhp rating at 5 psi equal to or greater than 8.8 bhp. Inter-
polation shows that the second line satisfies this condition at
about II bhp and 370 CFM. This will require the 15 hp motor.
This unit did not come with a variable speed drive and so a by-
pass valve was also acquired for flow control.
Step 3 - Determine total orifice area AQ according to the following formula:
A = Q (in2) in.2 x 6.45 = cm2
° 30
Where Q = blower air flow at 5 psi and mixing horsepower from
Figure 67.
Explanation^; This formula derives from the continuity equation,
Q = Av, solved simultaneously with the orifice equation
v = I,096 c / AP
Where v = orifice velocity, fpm
c = orifice coefficient
Ap = differential pressure across the orifice (inches of water)
P = density of air (assumed to be .0751bs/ft at standard
conditions).
The differential pressure used to calculate the above formulae was
just under 24 inches. Only about one foot would have been required,
however, it is necessary that the pressure never go below six
inches in the tank or there will be uneven aeration. The above for-
mula for sizing the holes will permit a significant reduction in
flow from design sizing before poor distribution will occur.
Examp 1 ej^ From the previous example:
A = 370 CFM , ,- . 2 ,. , ,2 , ._ 2
o —07: = 4.62 in (mches) x 6.45 = cm
332
-------
Step ^ - Design a header lateral system consistina of l5-20cm (6"--1") dia-
meter pipe headers v/ith 10 cm (4") diameter laterals connected as
shown in the typical examples in Figure 61.
Note : When laying out the pipes, leave room in the tank for an inlet
well and an outlet baffle as described in Section 6.5-5.
The following are criteria to be used in designing the header:
a. The 10 cm (V) dia. lateral pipes cover a good portion of the
tank.
b. A minimum length of lateral should be used so that when 0.5 cm
(3/16") to 1.3 cm (1/2") dia. holes are equally spaced along the
laterals, the hole spacings are not closer than 10 cm (V) apart.
Example : The smaller the holes, the smaller the bubbles, which 5s
good; however, the smaller the holes, the longer the required later-
als, which may be prohibitive to construct. Good judgment is re-
qui red.
2
Example: JL-_6_J_n_ ^°f^P-°l^~. 4 in _ ,_,. ,.
.027 in~2~per hole Xl2~7n7ft~ " ^ ^ ft'
for 3/16" holes
and
2
of holes *t in _ _
_
TTTnTft" ~ • '
for 1/2" holes
inches x 2.5'f = cun
ft x .305 = n
c. Any cross distribution header should have at least two headers
as shown in the C-, H-, and X- configurations in Figure 68.
6.6.16 Construction^ Steps: Aeration
Step I - Order a blower or blowers to provide the required air flow capacity
at 5 psi. See Section 7-6 if a rotary screw air compressor is used
A pressure regulator is needed to reduce pressure from 60 psi
down to required pressure. A bypass valve downstream of the pres-
sure regulator will be needed for flow control.
Step 2 - The tank size and aeration header configuration have been estab-
lished In the design section. The header may be constructed of
rigid steel or plastic pipe.
Step 3 ~ Drill the holes for the orifices a mint "nun; of 10 cm (V) apart
in the top side of the laterals. Do not drill the main headers.
333
-------
C - HEADER
CONFIGURATION
6"-8" DIA.
MAIN HEADER
4" DIA. PIPE
LATERALS
CONCRETE BLOCK
SUPPORTS
6"-8" DIA.
MAIN
HEADER
X-HEADER
CONFIGURATION
4" DIA. PIPE
LATERALS
V DIA. PIPE LATERALS
H-HEADER
CONFIGURATION
CONCRETE BLOCK SUPPORTS
^^y~
1— CONCRETE BLOCK
SUPPORTS
AIR FLOW
(FROM LATERALS)
MAIN HEADERS ARE SUPPORTED
ON BLOCKS
vii wh»wwr\*j
CONCRETE BLOCKS *
™» w w vi r»
\ '. • : ' •'
•
1 1 '
r ^
» i in in ii knv ki\
/
36"
I
?"QM
1^ 0
i-
t
j"
62-64"
,
INCHES X 2,54 + CM
EVALUATION VIEW
Figure 68. Aeration tank header alternative plan view
layouts and schematic of header support
33^
-------
Step k - Place the header into the tank and support it on six to ten
concrete blocks placed at positions as shown in Figure 68. Wire
the header to the blocks.
Step 5 - Piping from the header to the compressor should be kept as short
as possible. If a positive displacement blower is used no shutoff
valves or other restrictions which could terminate flow may be used
unless pressure relief is provided. In addition, a check valve is
needed or other means of preventing backflow of water through si-
phoning.
6^6.17 Operation and Maintenance: Aeration
Aeration systems are also operated on the basis of endpoint control. Chemical
reactions may take place either preceding or succeeding aeration using the
same steps indicated in 6.6.13.
Aeration for oxidation can be done using the following procedure:
I. Pump contaminated water into the tank.
2. Start the compressor and begin air flow, slowly at first, using
visual observation to determine proper air flow condition. Please
note that when the blower is shutoff, the air header manifold fills
with water (and debris). When the blower is turned on again the air
must purge the lines. This requires higher than normal pressures.
It would be desirable to refrain from shutting off the blower with
a full tank unless absolutely necessary.
3. Monitor the dissolved oxygen at various parts of the tank.
k. Continue aeration until a stable dissolved oxygen endpoint is
reached.
5. Pump contaminated water out of the process tank into the next process.
6. Desludge when the sludge layer reaches the top of the concrete
blocks to avoid clogging lateral holes.
6.6.18 Troub1eshoot?ng Aerat?on
Aeration times may be excessive so the following possible solutions are
presented:
Problem; Extremely long aeration times
Possible Solutions; 1) Clean holes in laterals; 2) Check for proper
compressor operation; 3) Repeat bench tests to determine if endpoint has
changed; A) Check temperature and barometric pressure to determine if the
saturation value has been reduced; 5) Determine if chlorination would be
more effective oxidation method by consulting technical advisor.
335
-------
7.0 CHAPTER 7 PROCESS COMPONENTS AND TREATMENT CHEMICALS
7.1 GENERAL
There are many components and materials which are common to all of the treat-
ment unit processes. Therefore, to avoid unnecessary repetition, these
components and selection criteria have been presented separately from the
construction details. This separation will require the user to cross refer-
ence between Chapters 6 and 7 frequently. Therefore it is mandatory that the
user be familiar with and understand the information presented in both
sections to allow proper use of this Manual.
The information presented here is intended as a guide and basic reference
on mechanical components. It is not a comprehensive review of all
possible materials. The information presented has been abbreviated and
simplified for use. Further information can be obtained from other
references. When equipment choices are made by the user, it is advised
that this choice be confirmed by equipment manufacturers or other
specialists in this field.
It was determined that the components section be broken down Into six
parts. These parts are summarized as follows:
Process Pump - (sizing and selection)
Process Tanks - (volume calculations and types)
Hoses, Valvlng and Fittings - (types and applications)
Chemical Feed Components - (requirements)
Blowers and Compressors - (types and sizing)
Materials of Construction - (types and application)
7.2 PROCESS PUMPS
Field implementation of treatment processes will require the availability of
pumps which are capable of moving the fluids under a variety of service
conditions. Successful implementation demands that properly selected
pumps be utilized to assure continuous operation and controllability of the
process. Careful selection is necessary because no one pump can meet all
service requirements and different pumps are available to meet different
needs. Care must be taken not to misapply a pump or failure may result.
336
-------
It is not possible to select a pump on flow requirements alone — other
important operating variables will have to be considered before a final
selection can be made, e.g., total dynamic head, suction conditions,
viscosity, solids content, power source, mobility requirements, corrosivity,
pumping explosive or flammable liquids, etc. The pump sizing and selection
criteria presented here are condensed and conservative to permit selections
without going through much of the detail normally involved in pump selections,
However it is not recommended to grossly oversize the pump, thus eliminating
the necessity of performing sizing calculations. Oversizing is generally
better than undersizing in emergency situations but with the drawback that
pumps lose efficiency and are not as controllable when operated above or
below their design ranges. Calculations of required flow and head permit
the selection of a pump which can operate in its efficient range. It must
also be carefully noted that the pump is not the only critical component
in a properly designed pumping system. Other factors such as line sizes and
flow restrictions, fittings, type of hose used, and the nature of the
operation and the substances to be pumped can determine to a large degree
the efficiency of the pumping system. A systems design approach, which
takes these important variables into account, will give the designer substan-
tial input concerning the nature of the system. This knowledge becomes
invaluable when dealing with problems which may occur. With the exception
of certain special pumping conditions such as the pumping of viscous fluids,
heavy solids loadings, or flammable or explosive substances, pump selection
may be made by first performing pump sizing (Section 7-2.1) and then turning
to the pump selection section (Section 7.2.2). Special pumping situations
are presented in Section 7-2.3.
7.2.1 Pump Sizing Procedure
The following procedure has been developed to assist in pump selection for
typical fluid transfer operations as part of field implemented treatment
systems. Assumptions are that the fluid is vapor-free, of low viscosity,
and with medium solids content. Inlet and outlet conditions are assumed to
be at ambient pressure and temperature conditions (57).
Step 1 - Calculation of System Flow Rate
Based on the volume of fluid to be transferred and the
required transfer time, system flow rate is calculated as
f o 1 1 ows :
337
-------
0 = — where Q = system flow rate, —— (gpm)
s t s mm
V = volume of fluid, m, (gal.)
t = t F me, m I n.
Step 2 - Determination of Pump Capacity
Establish whether the pump will be used continuously
(more than 8 hours per day) or intermittently.
Determine pump capacity, Q , as follows:
Continuous duty Q = 2xQ m /min (gpm)
Intermittent duty Q = 1.3xQ m /min (gpm)
Explanation: Pump capacity, Q , is only for ordering
purposes. All subsequent calculations will be per-
formed using system flow rate, Q .
Step 3 - Sketch of Pumping System
Sketch an elevation view of the proposed pumping
system (see Figure 69 and Table 29 for pertinent
pumping terms). Determine whether the suction port
will be flooded with fluid (Figure 69c) or whether
pump location will require a static suction lift
(Figure 69a). A static suction lift will require
a self-priming pump. Include the following information
on the sketch:
a) The vertical distance between the lowest supply
fluid level and the highest discharge water
level or the free discharge point. This defines
the Total Static Head (TSH).
b) For self-priming applications, indicate the
vertical distance between the lowest supply
level fluid level and the pump centerline.
This defines the Static Suction Lift (SSL).
c) Indicate the approximate total length of fluid
lines. Note how much is on either side of the
pump.
338
-------
DISCHARGE
FRICTION HEAD
STA
T
-$WT
TOTAL
DISCHARGE
>"4L_
STATIC
FRICTION HEAD
t TOTAL SUCTION HEAD
TOTAL
(a) SUCTION LIFT AND SUBMERGED DISCHARGE
T
1C
TOTAL
STATIC
HEAD .
STATIC DIS-
CHARGE HEAD
1
•A
'\\
TOTAL DIS-
PUMP
DISCHARGE CHARG
PUMP SHAFT
i HEAD
SUPPLY
(b) SUCTION LIFT AND FREE DISCHARGE
TOTAL
DYNAMIC
HEAD HEAD
T
TOTAL
STATIC HEAD
STATIC
SUCTION
HEAD
PUMP
STATIC FRICTION HE
JSnMGj1
STATIC DIS-
CHARGE HEAD-
PUMP SHAFT ,,
TOTAL DIS-
CHARGE HEAD
1
UCTION
(c) STATIC SUCTION HEAD AND SUBMERGED DISCHARGE
Figure 69. Examples of typical system sketches
showing pump head relationships
339
-------
TABLE 29. FLUID PUMPING TERMS
Static Suction Lift
Vertical distance in feet between the liquid
level of the source of supply and the center-
line of the pump when the pump is located
above the liquid level of the source of supply.
Static Suction Head
Vertical distance in feet between the liquid
level of the source of supply and the center-
line of the pump when the pump is located below
the liquid level of the source of supply.
Frictional Head
Pressure (expressed in feet) to overcome
friction and other losses such as fittings,
transitions and valves.
Total Suction Lift
Total pressure (expressed in feet) below
atmospheric at the suction port of the pump
when the pump is in operation (equals the
static suction lift plus the suction friction
head).
Static Discharge Head
Vertical distance in feet between the centerline
of the pump and the point of free delivery of
the 1iquid.
Total Suction Head
Total pressure (expressed in feet) above
atmospheric at the suction port of the pump
when the pump is in operation (equals the static
suction head minus the suction friction head).
Total Static Head
Sum of the static suction lift and the static
discharge head or the difference between the
static discharge head and the static suction
head.
Total Dynamic Head
Sum of the total discharge head and the total
suction lift or the difference between the total
discharge head and the total suction head.
Total Discharge Head
Total pressure (expressed in feet) above
atmospheric at the discharge port of the pump
when the pump is in operation (equals the static
discharge head and the discharge frictional head)
340
-------
d) Note on the sketch the location of valves,
fittings, elbows, entrances, enlargements, etc*,
(see Figure 70 for typical examples).
Step 4 - Preliminary Line Sizing
Using Table 30, determine a preliminary line sizing
for friction head calculations.
Explanation: Pump or line size availability may
later require an iteration of these calculations
starting with Step 4. Ultimate pump size is
affected by line size.
Step 5 ~ Computation of Total Dynamic Head
Use the form'presented in Table 31 to compute the
Total Dynamic Head.
Step 6 - Specifying Pump Rating
When ordering the pump, use the following information:
Flow equal to Qp (Step 2) at Total Dynamic Head from
Step 5. Also note whether a suction lift is required
and use the Total Suction Lift calculated in Step 5-
Table 30. PRELIMINARY LINE SIZING CHART
Line size, in.
0.75
1.0
1.25
1.5
2.0
2.5
3.0
3.5
4.0
5.0
6.0
8.0
10.0
Flow range, GPM
5
10
18
28
60
100
170
250
350
600
1000
2000
3800
- 10
20
- 35
- 60
- 120
- 220
- 350
- 500
- 720
- 1300
- 2000
- 4200
- 8000
1. Minimum represents a flow corresponding to 5 psi/
100 ft friction loss, maximum corresponds to 20 psi/
100 ft friction loss.
in. x 2.54 = cm
gpm x 3-785 = 1pm
341
-------
Globe Valve, Open
Gate Valve
M Closed
V4 Closed
14 Closed
Fully Open
Angle Valve, Open
Swing Check Valve
Fully Open
Close Return Bend
Standard Tee
Through Side Outlet
Ordinary Entrance
Standard Elbow or run of
Tee reduced '/6
Medium Sweep Elbow or
run of Tee reduced 14
Notr: For sudden enlarge*
menb or sudden contrac-
tions, uie the smaller
diameter on the nominal
pipe me scale.
Sudden Enlargement-
I «"/D-
d/b-V4
45' Elbow
Long Sweep Elbow or
run of Standard Tee
3000
2000
:1000
-500
300
200
-100
-i
-s
20 '£
c/S
48 —
-50
42-
36—
30-
22-
24—
20-
18-
16—
14-
12—
10
£ E ?--
O "~s.«7" —, — _ "
J
5 g
J
3 I
2
5— _
-1
iV4-
0.5
0.3
0.2
0.1
114-
'/i-
-30
20
10
-1
0.5
Use a straJghtedge to connect the type of restriction (left vertical line)
with the nominal size (right vertical line). Read the headloss in equiva-
lent feet on the center vertical line; e.g., a 6" standard elbow has an
equivalent loss of 17 ft. (see chart) (58).
ft x .305 = m
?n. x 2.5*1 a cm
Figure 70. Equivalent length of pipe fittings and valves
342
-------
TABLE 31. FORM FOR CALCULATION OF TOTAL DYNAMIC
HEAD (TDH) AND TOTAL SUCTION LIFT (TSL)
Explanation: Total Dynamic Head is needed to size
the pump; Total Suction Lift is needed as part of
the TDH calculation and to check the suction
restriction of the pump.
A. Determine system flow rate, Q (from Sizing Procedure, Step I)
GPM
B. Calculate Total Suction Lift or Total Suction Head (refer to
Figure 69).
a. Static suction lift, or Ft,
b. Static suction head Ft,
c. Suction friction head:
Fluid Line Head
(y)
(x) Friction Loss W~
Size Length Per 100 Ft. (psi) Total Line
(Inches) (Ft.) From Figure 71 ) _ Loss (Ft.)
Total Ft.
contInued
-------
TABLE 31 (continued)
Fitting Head
Fitting Size
Type Cinches)
(v)
_No._
(w)
Equivalent Length
Per Fitting (From
Figure 70)
(Ft.)
(v)-(w)-(y)
40
Total
Equivalent Length
(Ft.)
Total Ft.
c. Suction friction head = fluid line head Ft.
+ fitting head Ft. = Ft,
(a) + (c)
Specific Gravity
d. Total suction lift = ($L±Js) = Ft.
Explanation: If total suction lift is higher
than 15 feet, reduce it by:
1) Lowering the pump
2) Increasing the size of the suction
line and/or decreasing the over-
al1 length of 1ine
3) Eliminating unnecessary fittings
*0 Decreasing the flow
15 ft is the desired maximum condition
e. Total suction head = --4-~"--~- = _ Ft.
O * (j • : —- —
S.G. = Specific Gravity
cont i nued
-------
TABLE 31 (continued)
C. Calculate Total Discharge Head (refer to Figure 69)
f. Static discharge head Ft
g. Discharge friction head:
Fluid Line Head
(x)
Size Length
(Inches) (Ft.)
(y)
Friction Loss
Per 100 Ft. (psi)
(From Figure 71)
(x).(y)
~To
Total Line
Loss (Ft.)
Total
Ft,
Fitting Head
Fi tting
Type
Size
(I nchesj
(v)
No.
(w)
Equivalent Length
Per Kitting (From
Figure 70)
(Ft.)
Total
Equi valent
Length
(Ft.)
Total
Ft.
cont i nued
-------
TABLE 31 (continued)
Discharge friction head - fluid line head Ft.
+ fitting head Ft. = Ft.
h. Total discharge head = - v > = Ftm
J • VJ *
S.G. = Specific Gravity
i. Total dynamic head (TDH) « Total discharge head
+ total suction lift or total discharge head -
total suction head
TDH - (h) + (d) Ft.
or
TDH - (h) - (e) - Ft.
ft x ^305 = meters
-------
10,000
8,000
6,000
5,000
4.000
3,000
2,000
1,000
800
600
500
400
300
200
5 100
o 80
5 60
3 50
u- 40
30
20
10
8
6
5
4
3
2
1
08
0.6
05
04
m
FRICTION LOSS (HEAD), PSI PER 100 FT LENGTH
02 04 06081 2 3 4 56 8 10 20 40 6080
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FRICTION LOSS (HEAD), PSI PER 100 FT LENGTH
METRIC CONVERSION
ft x .305 » meters
gal. x 3.785 - Hters
psi x .0703
(REFER TO FIGURE 72 FOR USE OF GRAPH)
Figure 71. Friction loss In water piping (58)
-------
1.
Determine the head loss (psl/100 ft.) associated with a flow of
200 GPM through a V pipe. ________
o
300
200
100
0*
&
&
5 in.
k in.
3 In.
2 in.
Conversions
gpra x 3.785 - lpn»
ft x .305 - m -
psi x 703.1 - kg/n«
in. x 2.5k * cm
HEADLOSS (psI/100 ft)
READ HEADLOSS AS 1.5 psi/100 ft EQUIVALENT LENGTH
2. Determine the flow rate (GPM) to produce a minimum flow velocity of
3 ft./sec in a k inch line.
Q.
C3
3.
READ FLOW AS 120 GPM
Determine the line size (inch) to limit head loss to 5 psi/100 ft.
at a flow of 50 GPM.
3 in.
a.
C3
30
I
2 5 8
HEADLOSS (psl/100 ft)
READ LINE SIZE AS 1.8"
ROUND UP TO 2"
Figure 72. Typical determinations made from the
Friction Loss Chart (Figure 71)
-------
Examp1e:
Note: All calculations are In English units; the following conversions are
appropriate:
gal. x 3.785 - liters
In. x 2.5^ * cm
ft x .305 - m ^ f
25 ft. TOTAL OF PIPE,
WITH THREE ELBOWS
Size a pump to empty a ditch with an estimated capacity of 100,000
gallons in 8 hours. The fluid is water with a dilute contaminant and
a low solids content. The liquid will be pumped into a 10,000 gallon
swimming pool which will act as a pretreatment tank. Another pump of
equal or creater capacity will then pump to subsequent treatment
processes. A 4 inch diameter x 50 feet suction hose is available to
reach the low point In the ditch from a suitable location for installing
the pump. Sufficient pipe of verious sizes is available on site to make
the pump discharge connection Into the pool* Refer to Table 31a for com-
pilation of the results.
Step 1 - Calculation of System Flow Rate
V . 100,000 gal. Ihour
t o hours 60 mm.
Gf>M
Step 2 - Determination of Pump Capacity
Q » 2 x Q = M6 GPM (Continuous duty)
Step 3 ~ Sketch of Pumping System
The presence of a suction lift will require a self-
priming pump. The highest discharge point is the
top of the tank, 4 ft. above the pump centerline.
The lowest suction point is 12 ft. below the pump
centerline. The Total Static Head is 16 ft.
-------
TABLE 31a. COMPLETED FORM FOR CALCULATION OF TOTAL DYNAMIC
HEAD (TDH) AND TOTAL SUCTION LIFT (TLS)
Explanation: Total Dynamic Head is needed to size the pump; Total Suction
Life is needed as part of the TDH calculation and to check the
suction restriction of the pump.
A. Determine system flow rate, Qg (from Sizing Procedure, Step 1)
B. Calculate Total Suction Life or Total Suction Head
(refer to Figure 69).
a. Static suction 1ift
b. Static suction head
c. Suction friction head
Fluid Line Head
Size,
in.
(x)
Length,
ft
50
(y)
Friction loss
per 100 ft, psi
(from Figure 71)
208 gpm
ft
ft
ft
(x)-(y)
4o~
Total line
loss, ft
2.4
Fitting Head
TOTAL
2.4 ft
Fitting
type
ordinary
entrance
Size,
in.
4
(v)
No.
1
(w)
Equivalent length
per fitting, ft
(from Figure 70)
Total
Equivalent length,
ft
0.3
TOTAL
0.3 ft
Suction friction head = fluid line head (2.4 ft) + fitting head (0.3) ft
2.7 ft
continued
350
-------
TABLE 31 a (continued)
d. Total suction life
(a) + (c)
specific gravity
= 14.7 ft,
Explanation: If total suction lift is higher than 15 ft,
reduce it by:
1) Lowering the pump
2) Increasing the size of the suction life and/or decreasing
the overall length of line
3) Eliminating unnecessary fittings
4) Decreasing the flow
15 feet is the desired maximum condition
e. Total suction head =
(b) - (c)
specific gravity
ft,
C. Calculate Total Discharge Head (refer to Figure 69)
f. Static discharge head
g. Discharge friction head:
Fluid Line Head
Size,
i n.
3
Length,
ft
25
(y)
Friction loss
per 100 ft, psi
(from Figure 71)
8
4 ft
(x)-(y)
40
Total 1ine
loss, ft.
TOTAL
5 ft
Fitting Head
Fitting Size, (v)
type in. No.
elbow 3 3
sudden , .
enlargement
(w)
Equivalent length
per fitting, ft
(from Figure 70)
8
1.8
40
Total
Equ ivalent
ft
4.3
0.4
TOTAL
length ,
5.2 ft
cont inued
351
-------
TABLE 31 a (continued)
Discharge friction head • fluid line head (5 ft) + fitting head (5.2 ft)
- 10.2 ft
h. Total discharge head = ffl * ^ . = )4.2 ft
3 specific gravity
i. Total dynamic head (TDH) = total discharge head + total suction lift
or total discharge head - total sunction head
TDH - (h) + (d) 28.9 ft
or
TDH = (h) - (e) - ft
ft x .305 » meters
352
-------
Step A - Preliminary Line Sizing
From Table 30 choose a pipe which will be suitable on the
discharge for the preliminary calculation. A check of the
available pipe on site indicates that, of the two sizes, only
3" is available.
Step 5 - Computation of Total Dynamic Head
From form in Table 31a TDH = 28.9 ft.
Step 6 - Specifying Pump Rating
k\6 GPM at 28.9 ft TDH
Self-priming pump required
7.2.3 Selection of Available Pumps
The best local sources for suitable pumps to implement field treatment
processes are probably contractors' supply houses and contractors themselves.
They can supply pumps as well as limited lengths of hose. Secondary local
sources are the local sewage treatment plant, the department of public
works, and fire departments. Table 32 presents a selection chart based on
pump usage variables and available pump types. The type designations used
(A-D) will be found in other sections of this manual when referring to these
pump types. The following are descriptions and typical ratings of these
available pumps:
Type A - Medium pressure centrifugals
The most available variety is the self-priming, engine driven centri-
fugal pump. This type of pump is used by contractors in a variety of
sizes and ratings as shown in Table 33-
TABLE 33. TYPICAL RATING FOR MEDIUM
PRESSURE CENTRIFUGAL PUMPS
Size range (Inches)
Flow range (gpm)
Total head range (ft)
Horsepower range
Portable
1i - 3
25-350
20-140
3-7
Wheel
mounted
H - 8
20-2500
0-220
3-150
Skid
mounted
10
250-3750
30-120
100-150
Tractor
PTO
3-8
50-2000
23-^38
ft x 3-05 = m fpm x 3-785 = 1pm
in x 2.5k = cm hp x -7^6 = kw
353
-------
TABLE 32. PUMP SELECTION CHART
Pump Type Designation
Fluid Transfer -
med. pressure
high pressure
Sol ids hand!ing
3
I/I
1/1 —
z o
0)
i_
3 —
I/I ID
I/) O)
0) 3
I- M-
O- —
u
x: *J
o> c
._ «)
n: o
3
O
>
10 (0
O)
(0
Q.
n>
2. Suction Condition
Flooded suction
Suction 1i ft
Submersible pump
x
x
x
x
x
x
x
Power Source
Engine driven
Air driven
Electrical
Power takeoff
x
x
x x
x
x x
x
Mob i1i ty
Portable (by one to
three men)
Wheel mounted
Skid mounted
Tank truck mounted
x
X
X
X
X
X
X
X
X
X
X
-------
Although the pump is self-priming, an initial prime is required. A pipe
plug on top of the pump body must be removed and'the pumping chamber filled
with water. Even though it may run dry for a short period, the pump should
still hold its prime by virtue of the priming chamber design. The pump can
handle solids, but it is not a good choice as a solids pump because of
inaccessibility to remove fouling.
Another available centrifugal pump which finds extensive application in
dewatering is the electric submersible pump.
Typical ratings: English units Metric units
Size range 2-8 inches 5-20 cm
Flow range 50-2800 gpm 0.2-10.6 cu m/mln
Total head range 10-200 ft 3-61 m
Power 2-95 hp 1.5~71 kw
Type B - High Pressure Centrifugals
These engine-driven pumps are commonly used for high pressure
testing of plumbing systems. While not self-priming, they
are generally furnished with an exhaust or vacuum primer.
Typical ratings:
Size range 2.5-6 inches 6.3-15 cm
Flow range 50-1800 gpm 0.2-6.8 cu m/min
Total head range 70-460 ft 21-140 m
Power 5-125 hp 3-7~93 kw
Type C - Heavy Duty Trash Pumps
A readily available variety of solids handling pumps is the engine-
driven, self-priming, centrifugal, trash pump which has the same
variety of sizes, mountings, and ratings as the Type A - Medium Pressure,
Engine Driven Centrifugals. There are two major differences between
the medium pressure and the trash handling centrifugals:
The pump body and impeller of the trash pump are open to allow the
passage of large solids; solids ratings are given as the maximum diameter
of a spherical solid which the pump could pass:
Pump size Largest sphere passed
in.
1.5
2
3
Termed solids handling ability
355
cm
2.5
2.8-3.8
3.8-6.3
5-7.6
6.3-7.6
In.
1
1.1-1.5
1.5-2.5
2-3
2.5-3
-------
The self-priming trash pump is used on sanitary cleaning trucks, used by
septic tank cleaners and other waste fluid haulers. It is typically
available in 10.1 cm (V) size on a tank truck of 4.1, 6.0 or 8.3 cu m
(1100, 1600, 2200 gal.).
Another type designed for solids-laden streams is the electrical or
engine-driven diaphragm pump. This recirprocating pump utilizes a
flexible, elastomeric diaphragm which is flexed and extended by a
mechanical eccentric drive. Check valves are necessary to permit the
pulsing pump action. It is preferred to utilize hardwall hose on both
suction and discharge to minimize the surging forces on the hoses, hose
supports, and tanks. This pump is normaily available in the portable
and small wheel-mounted varieties with typical ratings as follows:
EnglIsh units Metric units
Size range 3-4 inches 7-6 cm
Flow range 50-150 gpm 189-568 1pm
Total dynamic head range 5~50 ft 1.5-15 m
Power 0.5-7 hp 6.4-5 kw
Type D - Mechanical and Pneumatic Diaphragm Pumps
This solids-handling pump usually comes in single diaphragm engine-
driven, portable varieties with the pumping action occurring because
of the reciprocal movement of a diaphragm driven by an eccentric.
Swing check valves on inlet and outlet permit fluid pumping. The
pulsing nature of the pumping can cause severe hose whipping if hoses
are not properly supported. Typical ratings are as follows:
Size range 3-4 inches 7.6-10.2 cm
Flow range 52-150 gpm 197-5680 1pm
Total head range 5~50 ft 1.5-15m
Power 2.75-6.6 hp 2.0-4.9 kw
Diaphragm pumps function best with a short suction line and low
suction lift.
Air Operated Double Diaphragm Pumps
The air-operated diaphragm pump is an excellent pump for solids handling
at higher head ratings than the typical mechanical diaphragm pump.
It is light weight, portable and self-priming, and may also be utilized
as a submersible pump. A single air pressure line is all that is
required for hookup, except in the case of the submersible pump, where
a vent line must extend above the water surface so that the air suction
of the pump does not fill with water when the pump is shut off. The
The pump has a reciprocal motion with pumping occurring by the movement
of the diaphragm controlled by an air valve and the opening and closing
of ball check valves on the inlet and outlet. It has a smoother motion
in many cases than mechanical diaphragm pumps. However, hose whipping
356
-------
must be controlled when using this pump also. The pump would be more
resistant to explosion or fire hazards than engine-driven or electric
motor-driven pumps. It could, however, freeze up in cold weather because
of the expansion of air in the air valve. The pumping rate can be easily
controlled by controlling air flow to the pump. Typical pump specifica-
tions are in the following table. (Table 34)
TABLE 34. TYPICAL AIR PUMP SPECIFICATIONS
Air requirements
Air
Pressure, consumption,
psig scfm
100 160
140
120
100
80
60
4o
20
2"
Flow,
gpm
110
58
28
12
Pumping
s i ze
Head,
ft
55
170
205
220
capac i ty
3"
Flow,
gpm
170
138
110
83
40
41
25
20
s i ze
Head,
ft
85
125
155
183
202
218
222
226
psig x 703 = kg/sq m
scfm x .028 = s cu m/min
gpm x 3.785 = 1pm
ft x .305 = m
Pumps can also be operated at lower pressures with varying pumping
capacities. Maximum solids size ratings are .63 cm (1/4") diameter for
a 5 cm (2n) pump and 0.95 cm (3/8") for a 7.6 cm (3") pump.
7.2.4 Special and Hazardous Pumping Situations
Special problems occur when handling viscous fluids, high solids content,
and flammable and explosive substances. Special care must be taken when
applying pumps for these situations because of the danger of failure or of
hazards to personnel.
7.2.4.1 Viscous fluids - Increased viscosity above that of water causes a
need for a higher pumping head than is needed to pump water at the same flow
rate. The viscosity of all fluids varies appreciably with changes in
temperature. The viscosity of some fluids is unaffected by the mechanical
motions occurring during transport (Newtonian fluids such as mineral oil
and water). A liquid is said to be thixotropic if viscosity decreases as
agitation is increased (asphalt, molasses). A liquid is said to be
dilitant if viscosity increases as agitation occurs (clay slurries).
357
-------
Because of the above complexities as well as the difficulty In getting
viscosity measurement in the field, it is not easy to establish a calculation
method to be used for field sizing of pumping systems for handling viscous
fluids. In the absence of a sizing technique, it is desirable to choose a
pump for viscous pumping service which has a head capacity substantially
higher than that which is necessary to pump water at the same rate. Ultimate
flow rate must be established in actual service. It is desirable when
pumping viscous fluids to reduce the number of restrictions and to keep
line velocities low and suction line length to a minimum.
7.2.4.2 Solids Handling - Again, calculation methods are not available for
solids pump sizing because of a number of factors such as: solids
concentration; viscosity; specific gravity; particle size; presence of
various constitutents such as silt, clay, sand, debris. Like the
viscous flow situation, an elevated head is needed to pump high solids
concentrations, but in addition a minimum transport velocity is
necessary to insure against solids settling in the lines. This
minimum velocity is in the range of 0.61 - 0.92 m/sec (2-3 ft/sec) and is a
function of line size and solids concentration.
If the cleanup operation will involve a major amount of dredging it
would be desirable to enlist the services of a dredging firm to advise
on the best pumping system configuration. Such items as suction line
backflush capabilities and pump and hose cleanout must be considered
to reduce downtime from clogged lines, pumps, and valves.
7.2.4.3 Flammable and Explosive Substances - Serious hazards can be created
by pumping systems when handling explosive or flammable fluids:
1. Ignition sources such as spark plugs, ignition wire
and switches, hot mufflers and engine blocks, combusttle
air filters, open electric motors, static electricity
buildup, are ever present dangers when using readily
available contractor's pumping equipment.
2) Pump suctions, and restrictions can cause gases to
be created in excess of the lower explosive limit
because of regions of reduced pressure.
Because of the imminent dangers of field implemented treatment systems
when dealing with dangerous substances, it is recommended that the
manufacturer of flammable or explosive substances be contacted
concerning safe ways to handle these products. In some cases the
dangers may preclude field treatment unless the substance can be
rendered less hazardous.
358
-------
7.3 PROCESS TANKS
The availability of process tanks is critical to the determination of
feasible system flow rates because of the detention times required by
the various process schemes. Unlike portable pumps, which are readily
available because of extensive requirements by contractors to dewater
construction sites, a limited variety of tanks are available which
could be turned to field treatment process uses. Some available tanks
include:
Open Top Tanks:
1. Commercially available above-ground swimming pools;
2. U.S. Army Corps of Engineers rubber stave tanks;
3. Impermeable membranes as liners for earthen excava-
tions or for steel, concrete, or wooden tanks;
k. Treatment of earthen excavations with high-swelling
clay to make the soil impermeable;
5. Culvert, storm, drain, and sewer pipe utilized for
vertical column tanks;
6. Specialized steel, fiberglass, and lined wooden tanks
borrowed from local Industries.
Closed Tanks:
1. ASME tanks with flanged and dished heads;
2. Tank trucks;
3. Collapsible rubber containers.
By far, the most practical tank for field implemented treatment pro-
cesses is the open top tank, which has the necessary accessibility for
operation and control of the process. For most processes, geometry is
not a critical parameter, with the notable exceptions of filtration,
carbon adsorption, and ion exchange. In gravity feed systems these
processes require vertical tanks of uniform cross-section and height-
diameter ratios typically greater than two. Closed tanks are mainly
limited to storage and transfer functions, such as clean effluent
storage for backwash or sludge storage and disposal. In an emergency,
process operations can be carried out in closed tanks, however, the
operation is tedious.
Tank sizing will require that the process volume for the various tanks
be known. The following section (Section 7-3.1) gives formulae for
calculation of process volumes for a variety of tank configurations.
Then, Section 7-3.2 presents a description of various available tanks
as well as some pertinent details concerning their installation and
use.
7.3.1 Calculation of Process Volume
Typical above ground and in-ground tanks have been classified in Figure 73
as specific tank designations (A-H). These type designations are used in
other portions of the manual when referring to specific tank types.
359
-------
TYPE A.
VERTICAL CYLINDER, FLAT BOTTOM,
OPEN TOP
D - DIAMETER, m (ft)
h • TANK HEIGHT, m (ft)
h - PROCESS HEIGHT, m (ft)
P
f - FREEBOARD, m (ft)
PROCESS VOLUME V -
TYPE B.
*D x h - 0.78D2 x h m3, (ft3)
P P
VERTICAL CYLINDER, CONE BOTTOM,
OPEN TOP
D - DIAMETER OF CYLINDRICAL SECTION,
m (ft)
h • TANK HEIGHT, m (ft)
h » PROCESS HEIGHT, m (ft)
fP- FREEBOARD, m (ft)
L - HEIGHT OF STRAIGHT SECTION,
LESS FREEBOARD, m (ft)
h - CONE HEIGHT, m (ft)
PROCESS VOLUME V
D (.?8L + .26 h ) m3, (ft3)
TYPE C.
L
r
h
f
L!
J
i
1
D
}
V -
P
ASME TANK, HORIZONTAL
D • DIAMETER, m (ft)
h - PROCESS HEIGHT, m (ft)
fp- FREEBOARD, m (ft)
L.- LENGTH OF STRAIGHT SIDE, m (ft)
L - TOTAL LENGTH, m (ft)
VH- VOLUME OF HEAD
(See Figure 7*0
.78D2L, + 2VH m3, (ft3)
I. THIS VOLUME IS TANK CAPACITY WITHOUT SUBTRACTION FOR FREEBOARD
Figure 73. Calculation information for tank volumes.
360
-------
TYPE D.
H
*P \
Vp • -52 Do
Do (0o'
CYLINDRICAL IN-GROUND TANK
(APPROXIMATION OF FRUSTRUM
OF RIGHT CIRCULAR CONE)
D - OUTSIDE DIAMETER, m (ft)
D?« INSIDE DIAMETER, m (ft)
h - TANK HEIGHT, m (ft)
h - PROCESS HEIGHT, m (ft)
fp- FREEBOARD, m (ft)
m3, (ft)
TYPE E.
RECTANGULAR IN-GROUND TANK
(APPROXIMATION OF OBELISK)
(ELEVATION VIEW SIMILAR TO D
ABOVE)
OUTSIDE LENGTH, ra (ft)
INSIDE LENGTH, m (ft)
OUTSIDE LENGTH, m (ft)
W? INSIDE LENGTH, m (ft)
h TANK HEIGHT, m (ft)
PROCESS HEIGHT, m (ft)
FREEBOARD, m (ft)
Vp - I [Vo + (Wo * W«) (Lo + L!) * W.Ll] x h m3, (ft)
b P
Figure 73 (continued). Calculation information for tank volumes.
36)
-------
TYPE F.
W
L
h
WIDTH, m (ft)
LENGTH, m (ft)
TANK HEIGHT, m (ft)
PROCESS HEIGHT, m (ft)
FREEBOARD, m (ft)
FOR SQUARE W - L * SIDE, m (ft)
• WLh
P
m
(ft3)
TYPE G.
Vp - .78DL
m
(ft)
VERTICAL CYLINDER, ASHE FLANGED
AND DISHED HEAD ON BOTTOM
D • DIAMETER, m (ft)
L « LENGTH OF STRAIGHT SECTION
LESS FREEBOARD, m (ft)
h - PROCESS HEIGHT, m (ft)
fp- FREEBOARD, m (ft)
h - TANK HEIGHT , .
VM- VOLUME OF HEAD, nT (ft*)
" (See Figure 7*0
TYPE H.
VERTICAL, OVAL-SHAPED CYLINDRI-
CAL TANK
W
L
h
f
h
- [W x L - .22VT] x h
WIDTH, m (ft)
(diameter of round end)
TOTAL LENGTH, m (ft)
TOTAL HEIGHT, m (ft)
FREEBOARD, m (ft)
PROCESS HEIGHT, m (ft)
m
(ft3)
Figure 73 (continued). Calculation information for tank volumes.
362
-------
luuu
800
600
500
300
200
100
« 80
S. 70
. 60
"». 50
§ 30
o 20
10
6
5
3
2
METRIC CONVERSION
ft x .305 » m
gal. x 3-785 - 1
2n
DIAMETER OF TANK (ft.)
Figure 7^. ASTM head volumes
363
-------
The calculation for process volume allows for freeboard, which is a process
requirement. Determination of freeboard must also take into account the
hazard associated with the fluid, the structural stability of the tank,
imminent dangers of leaking or overpressurization and the controllability
of the process against overflowing.
7.3.2 Available Tanks - Description and Installation
The following tanks may fit a variety of process requirements. They were
chosen on the basis of availability as well as desirability. It will be
noted that .some tanks most suited for field implemented treatment schemes
are probably not locally available, e.g. rubber stave tanks. They are
included however, to emphasize the need to make suitable process equipment
available to facilitate field-implemented treatment.
Installation details are presented here to allow the user to:
1. Be aware of special requirements for tanks.
2. Allow tank choice based on installation requirements and site
considerat ions.
3. Become familiar with actual methods of installation.
7.3-2.1 Type A - Above Ground Swimming Pools - There are many types of
commercially available pools but the most practical variety utilizes a
flexible liner (usually 0.5 mm (or 20 mil) vinyl), finished steel sheet
sides, and aluminum pedestal supports.
The pools typically come in circular shapes from 4.6 - 8.5 m (15~28 ft) in
diameter and from 1.2 - 2.1 m (4-7 ft) deep. Allowing a minimum of 15 cm
(6") freeboard, this represents a process capacity range of from 17-5 -
113-2 cu m (620-4000 ft^). The pools are also typically available in oval
shapes from 3.7 x 7.3 m (12 x 2V) overall, to 4.9 x 12.2 m (16 x 40') over-
all, at 1 .2 - 2.1 m (4-71) deep. This represents a process capacity range
of from 25.5 - 107.6 cu m (900-3800 ft3). They can probably be set up on
a prepared site by three men in four hours. Four specific precautions
are necessary in the field use of these tanks:
1. They should be set up on as flat a surface as possible with a solid
base under the pedestal supports.
2. A smooth undersupport for the liner is necessary, with all sharp
objects removed. It is preferred to support the liner above
5-10 cm (2-4") of sand or to install a ground cloth below the
liner for insurance when on an uneven surface.
3. A 15 x 15 cm (6 x 6") curved fillet of sand is necessary to provide
a radius of support for the liner at the juncture between the
bottom and the walls. (See sketch on following page.)
4. Whenever a process component is introduced into the tank, e.g.
hose thrown over the side, submersible pump installed on the
bottom, etc., a piece of rubber or thick plastic should be
installed to protect the liner from puncture.
364
-------
_. SAND FILLETS
L. A
SIDE ELEVATION VIEW OF
TANK SHOWING RADIUS
FILLETS OF SAND
15 cm (6")
15 cm (6")
Installation steps can be summarized as follows:
1. Choose a flat and open surface for instal 1 atior\.
2. Remove protruding objects, and place 5-10 cm (2-^ In.) of sand or
a heavy ground cloth over chosen area to prevent rupture.
3. Build sand fillets around the radius of the pool.
4. Install pool (see Instruction Manual provided with pool).
5. Place protective liner inside the pool for added safety.
7.3.2.2 Type A - U.S. Army Corps of Engineers Portable Tanks - There is an
open top tank with far better field implementation possibilities than the
swimming pool, but with limited availability. This is the Army Corps of
Engineers Collapsible Water Tank. This tank comes in two sizes: 5-7 and
11.A cu m (1500 and 3000 gal.) A modified version of this tank in the
568 cu m (15iOOO gal.) size has been used very successfully in the
hazardous spills trailer treatment system. Tank construction is neoprene
coated nylon material which is a tough, corrosion resistant material. The
tank can be set up almost anywhere, is not easily susceptible to puncture,
and has tank fittings to accommodate process hookups. Instead of the alumi-
num sidewall pedestals used by the swimming pool for support of the liner,
the stave tank uses wooden slats which are quickly installed through stave
pockets in the tank walls.
On soft or wet ground, boards would be placed under each stave to prevent
sinking of the staves, which could result in their bowing out and cracking.
Ground surface preparation involves removal of protruding objects which
could puncture the liner. Spreading of 5-10 cm (2-k inches) of sand under
the tank can provide insurance against such punctures as well as use of the
rubber ground cloth which comes with the tank.
Support bars span the top of the tank to maintain a circular cross section
and guy ropes provide restraint against tipping. They can be fastened
with stakes or just tied to water-filled or sand-filled barrels. The
tank comes with a repair kit should a material failure occur. After
disassembly, the tank, staves, and poles can be stored in a relatively
small container.
Installation can be summarized as follows:
365
-------
1. Choose appropriate site (flat/open)
2. Remove protruding objects and place 5~10 cm (2-4") of sand under
tank to provide safe base.
3. Install tank (see instruction manual provided with tank).
4. If the ground is wet or soft, place boards under each stave.
5. Add support bars and secure guy ropes.
7.3.2.3 Types A, D, E, F, G Impermeable membranes as liners for earthen
excavations or for steel, concrete, or wooden tanks - Synthetic flexible
membranes have been long used as swimming pool liners and tank liners for
water softeners but more recently are being used extensively in lining of
ponds and canals, and in many other types of earthen excavations. New
materials are being introduced regularly but at the present time, PVC,
polyethylene, EPDM rubber, Hypalon, and chlorinated polyethylene, either
with or without reinforcements are finding applications. The liners are
available in large sheets with the exception of pool liners (20 gauge vinyl)
which may be specially constructed to fit a certain size excavation. Where
sheets are used in small excavations, a number of ruffled folds are necessary
to make the flat sheet fit the contour, but this is not detrimental to
process treatment. In large excavations, overlapping and sealing of the
sheets is necessary. The differences between the available materials are
summarized in Table 35-
Many of the polymers are produced with fabric reinforcements, varying
from light-weight nylon scrims to very heavy nylon or polyester scrims,
producing a variety of material strengths.
The earth Itself has to be loadbearlng in order to support the weight of
the water and the membrane's function Is to make the ground impermeable.
It is necessary to remove all debris which might cause damage, Including
stones, roots, etc. A sand layer base of 5~10 cm (2-4") Is desirable.
When forming the sand on Inclined surfaces the sand should be wetted
and trowelled if possible.
When liner sections are overlapped, the water pressure tends to
stabilize the joint by compression, minimizing seepage through Improper
joints.
The following summarizes the Installation procedures:
1. Choose or excavate appropriate area.
2. Remove debris.
3. Place a sand layer 5-10 cm (2-4") thick If possible - wet and trowel
sand on inclined surfaces.
4. Place and seal liner in place (see instructions accompanying
liner).
7.3.2.4 TypesJ) and E - Excavations treated with highly colloidal clay - This
method of converting an excavatTon into a sealed tank involves treating
the upper layer of soil with a clay which, when wetted, swells many times
its volume and forms an impermeable seal. The material, called volclay, or
bentonite, consists chiefly of hydrous aluminum silicate and is mined
366
-------
TABLE 35. SYNTHETIC LINER MATERIALS
Material Thickness Guage
Polyethylene 2-8 mi Is light
Polyvtnyl
Chloride
Butyl and
EPDM Rubber
Hypalon and
Chlorinated
Polyethylene
Vinyl
8-40 mi 1
30 mil
8-35mil
Length Width
any up to 40'
heavier
up to
700 ft.
32-125 mil medium
any
medium
any
light
any
up to 70
80 ft.
20 ft.
4-20'
4-61 ft.
Seal ing Method
heat or adhesion
solvent made
heat
solvent
heat, solvent or
adhes i ve
Comments
1. least expensive
2. fairly stiff and
may not conform
to irregularities
3. heat seal is best
but difficult to
do in the field.
1. much stronger
and tougher than
all
2. Good bonding
3. Expensive
1. Difficult to
seal since it is
a vulcanized
product
2. Moderate tough-
ness and puncture
resistance
3. highly extensible
1. intermediate
strength elongation
and toughness
2. easily avallable
in large panels
1. normal swimming
pool liners
2. excellent puncture
resi 5 fence
-------
almost solely in the Black Hills region of the U.S. Information on the
availability of product may be obtained from:
American Colloid Co.
5100 Suffield Court
Skokie, Illinois 600?6
The material may be loaded onto a bulk lime fertilizer spreader to
apply a uniform cover of the material over the tank area. Using a farm
disk, Volclay is mixed into the top 5~7.6 cm (2-3") of soil. The
Volclay-soil mixture is returned to its approximate original density
with a wobble-wheel or steel wheel roller before being wetted. For
small tanks, the above operations could all be performed by hand.
Caution. Care must be taken, however, to wear respirators to prevent
excessive inhalation of the submicron clav dust.
7.3<3 Column Tank Options
Type A column tanks for filters, carbon columns, and ion exchange columns:
A. Tanks constructed of corrogated steel pipe.
This piping is generally available in 20 foot lengths in the
diameters and gauges shown in Table 36. Where fittings are to be
installed on the tank or other welding is to be done, \k gauge or
lower is preferred. Pipes can be cut to desired tank height.
B. Tanks constructed of reinforced concrete culvert, storm, drain,
and sewer pipe (see Table 37).
Caut Jon: Be sure to use reinforced concrete to avoid excessive
strain in the column.
When 0-ring gaskets are used, it may be desirable to stabilize the
tank by nailing several 2x4 wood straps across the joint at spaced
intervals around the periphery.
C. Foundations for Column Tanks
A base of reinforced concrete must be poured for each column tank.
These foundations are to be placed on firm soil. Field tests to
determine firm soil on the basis of soil strength and density are
shown in Table 38.
368
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TABLE 36. INFORMATION ON CORROGATED STEEL PIPE (59)
Corrugation & Diam.
2 2/3" x 1/2"
& 2" x 1/2"
12 in.
15
18
21
2k
27
30
33
36
42
48
54
60
66
72
78
84
90
96
3" x 1"
36 in.
42
48
54
60
66
72
78
84
90
96
102
108
114
120
End Area
Sq. Ft.
.79
1.23
1.77
2.40
3.14
3.98
4.91
5.94
7-1
9-6
12.6
16.0
19.6
23.8
28.3
33.2
38.5
44.2
50.3
56.7
63.6
70.9
78.5
** Gages
Avai 1
18 16
.052 .064
* A
A *
A A
A A
* A
JU
*
A
A
A A
A
A A
A
A A
A A
A A
A A
A A
A A
j. -i
A A
A
A
and Th
able in
14
.079
A
A
•V
A
JU
A
A
A
A
JU
A
A
A
A
A
A
A
A
A
A
A
A
A
A
A
j.
A
A
icknesses
Inches
12
.109
A
A
?'c
JL
A
J.
A
ju
A
A
A
JU
A
A
JU
A
A
A
A
A
J.
A
A
A
A
A
A
A
A
10
.138
JU
A
A
**%
A
A
A
JU
f+
A
A
A
A
A
A
A
A
A
J.
A
A
j.
A
JU
A
A
A
8
.168
A
A
JU
A
A
A
A
A
A
A
A
A
A
A
JU
A
A
A
A
A
A
A
JU
JU
A
in. x 2.54 » cm
sq ft x 0.093 » sq m
369
-------
TABLE 37. REINFORCED CONCRETE PIPE INFORMATION
WALL
Internal Minimum Wai
Diameter, Thickness,
inches inches
12 1 3/4
15 1 7/8
18 2
21 21/4
24 21/2
27 2 5/8
30 2 3/4
33 2 7/8
36 3
42 3 1/2
48 4
54 4 1/2
60 5
66 5 1/2
72 6
78 6 1/2
84 7
90 71/2
96 8
102 8 1/2
108 9
Internal
Diameter
inches
114
120
126
132
138
144
150
156
162
168
174
180
inches x 2.5^ » cm
Ibs x b5h a kg
A
1 Average
Weight .pounds
per foot
79
103
13V
171
217
255
295
336
383
520
683
864
1064
1287
*•* 1532
1797
2085
2395
2710
3078
3446
Large Sizes
Internal
Diameter
feet
9 1/2
10
10 1/2
11
11 1/2
12
12 1/2
13
13 1/2
14
14 1/2
15
WALL B
Minimum Wall Average
Thickness, Weight .pounds
inches
-2
2 1/4
2 1/2
2 3/4
3
3 1/4
3 1/2
3 3/*»
4
4 1/2
5
5 1/2
6
6 1/2
7
7 1/2
8
8 1/2
9
9 1/2
10
of Pipe Tongue
Wall
Thickness
inches
9 1/2
10
10 1/2
11
11 1/2
12
12 1/2
13
13 1/2
14
14 1/2
15
per foot
93
127
168
214
264
322
384
451
524
686
867
1068
1295
1542
1811
2100
2409
2740
3090
3480
3865
and Groove
WALL
Minimum Wai
Thickness,
inches
.
-
-
-
3 3/4
4
4 1/4
4 1/2
4 3/4
5 1/4
5 3/4
6 1/4
6 3/4
7 1/4
7 3/4
8 1/4
8 3/4
9 1/4
9 3/4
10 1/4
10 3/4
Joint
Average
C
1 Average
Weight .pounds
per foot
.
-
-
-
366
420
476
552
654
811
1011
1208
1473
1735
2015
2410
2660
3020
3355
3760
4l6d
Weight, pounds
per foot
3840
4263
4690
5148
5627
6126
6647
7190
7751*
8339
8945
9572
Concrete pipe is available In 2.M m (81) lengths, a variety of diameters.
and In three wall thlckenesses. Wall A is preferable because ft is the light-
est and makes the pipe easiest to handle. Pipe joints are tongue and grooved
and can be joined with mortar or gasket package as well as with 0-rjng
gaskets to form tanks of desired height. Required sections greater than
2.kk m (81) high can be obtained by sawing the concrete Into desired
lengths, and then stacking them together.
370
-------
TABLE 38. SOIL STRENGTH AND DENSITY INDICATORS
Term
SOIL STRENGTH
Unconfined Compressive
Strength (After
Terzaghi and Peck)
Field Test
(After Cooling, Skempton,
Glossop)
and
Very soft 0-0.5 kips per sq. ft,
Soft
Fi rm
Stiff
Very stiff
Hard
0.5-1.0
1.0-2.0
2.0-3-0
3.0-4.0
4.0 or more
Squeezes between
is closed
Easily molded by
Molded by strong
Dented by strong
fingers when fist
fingers
pressure of fingers
pressure of fingers
Dented only slightly by finger pressure
Dented only slightly by pencil point
Term
Re 1 a t i ve
Densi ty
SOIL DENSITY
Field Test
Loose
Fi rm
Dense
0-502
50-70
70-90
Very dense 90-100
Easily penetrated with 1/2-in.
reinforcing rod pushed by hand
Easily penetrated with 1/2-in.
reinforcing rod driven with 5~lb.
hammer
Penetrated a foot with 1/2-in.
reinforcing rod driven with 5~1b«
hammer
Penetrated only a few inches with 1/2-
in. reinforcing rod driven with
5~lb. hammer
kips x .454 x 10"3 - kg
sq ft x .093 = sq m
in. x 2.54 m cm
371
-------
Concrete pad details are as follows: 20 cm (8") thick square pads
with base dimensions for various tank diameters are as follows:
m
inches m x m inches
0.61 2k
0.76 30
0.91 36
1.07 42
1.22 48
1.37 54
,22 x 1.22 48 x 48
,32 x 1.32 52 x 52
.42 x 1.42 56 x 56
.52 x 1.52 60 x 60
.63 x 1.63 64 x 64
.73 x 1.73 68 x 68
1.52
60 1.83 x 1.83 72 x 72
Woven wire recinforcement is to be placed near the bottom of the slab.
After pouring the slab, but before the concrete gets stiff, the tank Is
to be placed on the center of the pad and allowed to sink 7-6 cm (3")
Into the concrete. This will form a water seal at the base. It is
very important that the tank be supported in a vertical orientation
until setting occurs.
Holes through the concrete tanks for fittings (preferably threaded
nipples) can be installed using a chisel. The nipple can then be
mortared in. Metal tank fittings can be welded in place.
D. Installation of Column tanks.
1. Choose a suitable location - be sure that firm ground is
chosen to prevent the column from moving.
2. Prepare area and pour concrete slab (see previous section
for details)-
3. Allow concrete to partially set and then place column in the
pad.
Caution: Be sure that the column is supported vertically
until the concrete is set. Possible methods would be to
place concrete blocks under the column or provide support.
k. If additional height (for concrete columns only) is necessary,
use the following procedure:
a. Cut column to desired height with a concrete saw.
b. Place gasket, O-rlng or mortar around the groove on the
base column.
c. Put column extensions on top of column and seal cracks
with excess mortar (trowel smooth).
d. Provide extra support around the joint.
5. Wooden braces can be used to reinforce the column if necessary.
6. Chisel holes through concrete for fittings and mortar connections.
372
-------
7.3. ^ Col lapsible Rubber Tanks
These tanks are very handy for treatment systems effluent storage and back-
wash storage. They are typically available in neoprene and Buna-N in sizes
ranging from 1.89 - 37-85 cu m (500-10,000 gal.). The tanks come fitted
with inlet and outlet fittings. They must be used with a filler vent pipe
installed for air venting and to prevent overpressurizat ion. As in other
rubber tanks, care must be taken to prevent puncture from sharp objects. A
ground cloth or layer of sand is advised.
l.k PROCESS FLOW COMPONENTS AND FLOW CONTROL
While tanks and pumps are of primary concern in process system construction,
process flexibility and control is provided by other components as well,
such as piping, hoses, tubing, valves, etc. Selection of these components
is of prime importance if the pumps and tanks are to be used effectively.
It is impossible in a short space to summarize all of the plumbing devices
and installation methods which could be utilized to achieve proper process
connections. In almost all localities the availability of plumbing
contractors is a valuable resource for expeditious installation of plumbing
systems .
This section will provide information on simple connections using hoses
and basic control techniques. Plastic piping Is also described for use
!n very corrosive situations. Simplicity Is desired in field operations
for process flexibility ease of operation and maintenance. However, in
terms of safety from hazards, the simplest system may often be the most
dangerous. For example, It Is probably possible to interconnect processes
without the use of valves in many cases. But the constant manual shift-
ing of hoses Is a time-consuming and potentially dangerous operation
when extremely hazardous materials are being handled. Discretion and
good judgment are required in designing a plumbing system which Is
feasible In the particular situation, as well as being safe.
7.^.1 Hose, Tubing, and Fittings
7. A. 1.1 Process Hosing - Hoses for this service can generally be selected
according to the following criteria:
a. Suction or discharge (vacuum or pressure)
b. Necessary configuration and use
c. Pressure rating
d. Materials of construction
Information on commercially available hoses are presented in Table 39.
Suction hose is very useful in a spill treatment system. It is the
most versatile hose in terms of being able to be used interchangeably
for suction or discharge in almost any configuration. There Is little
concern with kinking, however this hose can be damaged by vehicular
traffic. It is rather costly and heavy to handle. The hose has
excellent aval labi 1 1 tv. Another suction hose which is less available
373
-------
TABLE 39. COMMERCIALLY AVAILABLE HOSES
Tube
Hose Description Material
Suction Hose
Water Suction Neoprene
(Rubber cover and
tube, wi re wound)
Heavy Duty Plastic PVC
(Black colored)
Rated
Pressure (Psi)
Avai lab
Length
Psi
Ft.
Psi
"
Ft.
i ,-,
te '
(Ft.) 1.5 2.0
(Full Vacuum to Positive
Pressures as Shown)
100 100
50 50
130* 115
75* 65
60 60
Diameter (in.)
2.5
100
50
100
65
60
3-0
100
50
85
45
60
4.0
100
50
75
40
60
6.0
50
20
60
35
20
Avai la"
bility
Excel lent
Med i urn
Discharge Hose
(Positive Pressure Only)
Rubber Discharge
(Rubber cover and
tube) 4 Ply SBR/EPR
3 Ply
Mill Hose
Rubber Lined,
Cotton Jacketed "
(50 Ft. Lengths)
Synthetic Yarn PVC
Plastic Impregnated
* Pressure rating at 72°F
Pressure rating at 150°F
Psi
250
225
150
125
125
110
Medi urn
" Not Pressure Rated
Ft.
Psi.
Ft.
Psi
Ft.
100
200
50
75
300
psf x 703 -
ft x .305 -
50
200
50
60
300
kg/sq m
m
50
200
50
55
300
50
200
50
50
300
50
200
50
40
300
50
200
50
40
300
Excel lent
Med i urn
m x 2.54 "cm
-------
but lighter in weight is the plastic suction hose. It is preferred to use
the heavy duty variety (often black in color). Pressure ratings are
affected by temperature for the plastic hose and it can pull a full vacuum
only up to ^9°C (120°F). It becomes somewhat stiff at cold temperatures.
Discharge hose Is lightweight and inexpensive, but not versatile for use in
connecting pumps or treatment processes because of kinking. It becomes very
useful for pumping long distances, e.g. raw flow and final effluent
discharge. These long runs can be carefully laid and then left uninterrupted,
It is desirable to use a short section of suction hose on either end of the
long run where connection to a pump or into a tank could product a kink.
Of the various types of discharge hoses, mill hose is the most readily avail-
able, is economical, and is lightweight.
Process hose support and protection must be handled very carefully. The
following are some precautions that should be taken:
1. Tie all free hose ends so that the hose cannot become free or
change configuration causing spillage. These supports should
be rechecked after hose filling because a hose takes on
additional weight when water filled. Tying down hoses is
extremely critical when utilizing free discharge into a tank
from a diaphragm Dump or other type of reciprocating pump.
Hose whipping can injure personnel and tank linings as well
as spraying contaminated water.
2. When laying suction hoses across areas of vehicle access,
the noses should be either buried or strattled with planks.
These planks should be pinned to the ground or otherwise sup-
ported to prevent movements. These precautions will prevent
wire-wound hoses from crushing and causing flow restrictions.
7.^.1.2 Process Hose Fittings - The following readily available fittings
are quite suitable for connecting hoses in field implemented pumping systems.
They come with shank ends for mounting to hoses or pipe threads for
connecting to process components such as pumps and tanks.
1. Quick couplings - adapter slips into coupler and then is sealed
against a gasket by moving two cam-actuated arms; quick to re-
move and versatile; readily available in brass, alumimum, and
cast steel .
2. Pin lug couplings - use a pin lug swivel nut to tighten joint;
requires two spanner wrenches; good for hoses which are not
often separated during operation; readily available in brass,
aluminum, and cast steel.
3. Combination nipples - a shank to pipe thread adapter; for hose
pipe thread connections that are typically not removed during
the process operation; readily available i'n cast steel.
375
-------
7..*K 1.3 Process Hose Clamps - Clamps include two basic varieties: one
requiring a special tool, such as Band-It or Punch-Lok clamps, and one
requiring only a screwdriver or wrench, such as worm gear clamps or two-bolt
clamps. The band material is available in coated steel or stainless steel.
The clamps requiring the special tools are often better suited for handling
of hazardous fluids because of the leverage which can be applied resulting
in a strong clamping. It is preferred to use two clamps per hose end to
assure trouble-free operation. It Is necessary to attach the clamps on the
hose shank portion of the fitting.
7.^.1.A Installation of Fittings on Hoses - The following are recommended
steps for field Installation of fittings (normally requires two people):
1. Lubricate the shank portion of the fitting and the inside of
the hose with a light oil (preferred) or water.
2. Cut the hose off square with a hacksaw. (Wire-wounded hoses
can be cut with a hacksaw, but it is somewhat tricky).
3. (Plastic hardwall hose only) Heat the hose end by immersion in
hot water for several minutes.
k. Have one person hold the free hose end vertically upright.
5. The second person can install the fitting, and drive it down
into place with a hammer or heavy tool. Do not hit the fitting
with a metal tool; cushion the blow by placing a piece of wood
in-between.
6. Whenever possible, continue to drive on the fitting until the
hose contacts the shoulder on the fitting. The main concern is
to have several of the shank bars inside the hose for good
clamping.
7.A.I.5 Plastic Pipe and Fittings - Although not as readily available as
steel piping, plastic piping and fittings are very useful when pumping corro-
sives, or when forming manifolds for aeration. Available materials include:
1. PVC (Polyvinyl Chloride) - A very strong plastic pipe: maximum ser-
vice temperature of 60°C (l40°F). Excellent chemical resistance
to a wide range of corrosive fluids, but may be damaged by ketones,
aromatics and some chlorinated hydrocarbons; is joined by solvent
welding or threading.
2. CPVC (Chlorinated Polyvinyl Chloride) - Can handle corrosives up
to 85°C (185°F). Comparable to PVC in chemical resistance; is
joined by solvent welding or threading.
3- Penton (Chlorinated Polyether) - Very good chemical resistance and
is useful up to 121°C (250°F). Costs two to three times as much as
PVC piping and is used for elevated temperatures or where other
376
-------
materials lack satisfactory resistance to specific chemicals;
is joined by threading.
*». Polypropylene - Finds wide application in pumping mixtures of acids,
bases, and solvents; may be used up to 82°C (180°F); is best joined
by Thermo-Seal fusion welding.
A variety of fittings, e.g. elbows, tees, couplings, reducers, flanges,
etc. are available in both threaded and socket types. Local stocking of
pipe and fittings, however, will probably be limited to PVC products.
Plastic piping is installed to look very much like metal piping
systemswith the difference that closer support spacings are required.
The following is a brief description of joining methods for plastic pipe:
1. Solvent Welding - The generally preferred method of joining rigid
thermoplastics such as PVC and CPVC, is solvent welding. This
gives a stronger joint than threading and is also considered faster
and simpler. Additionally, solvent welding permits the use of
thinner walls, when compared to threaded connections, for equiva-
lent pressure ratings.
2. Threading - As is the case with metal pipe, threading reduces the
effective wall thickness of thermoplastic pipe and introduces
notch effects which lower strength. Threaded connections should
be used with Schedule 80 or heavier pipe. The chief advantage of
threading is the ease of disassembly it offers.
3. Thermal Bonding - By taking advantage of the thermoplastic!ty of
the materials, methods of joining solvent-resistant thermoplastics
such as polypropylene are available which utilize tools to apply
regulated heat uniformly and simultaneously to pipe and fitting
mating surfaces so that true melting occurs on the surfaces.
Only hand pressure is needed to join the components and as the
material cools, a permanent homogenous bond results.
k. Flanging - One of the earliest methods for joining thermoplastic
piping, flanging continues to be used extensively for process
lines. Thermoplastic flanges and flanged fittings are available
in a full size range and may be attached to pipe by solvent
welding, by threading, or by thermal bonding, as required by the
particular thermoplastic material.
7.^.2 Flow Control
Tanks, pumps, hoses, and fittings constitute the primary means to store,
move, and treat fluids in field implemented process systems. However,
because not all pumps are variable speed controlled, and because treat-
ment processes involve flow diversions to accomodate the various process
377
-------
modes, vaTves or other flow control devices will probably be required
In most treatment systems. If they are not required for flow control,
they are desirable from the standpoint of safety. For example, when
treating hazardous fluids, it is preferred from a safety standpoint, to
open or close a valve rather than manually changing hose locations and
connections. in this manual, no attempt was made to devise valving
systems to eliminate hose transfers in the various process modes. Since
the local avalabllity of valves Is unknown, it would be advisable for
the On-Scene Coordinator to have the services of a person versed in
design and construction of plumbing systems for hookups.
The following are flow control techniques which can be employed in field
treatment systems:
1. Pump speed control - flow control may be inherent in speed
controls which are built in the pump-drive system itself. For
example:
a. Engine driven pumps - engine throttling Is used to alter
pump speed and thus control flow;
b. Air-driven pumps - control of air flow is used to regulate
fluid flow;
c. Variable-speed electric pumps - mechanical linkages between
motor and pump allow variable drive ratios which alter pump
speed and change flow.
2. Changing of pump head-Most di rect-coup led electrical pumps, how-
ever, will be constant-speed devices and require changes in
pressure head to control flow. A variety of pump head control
techniques are possible:
a. Throttling valve control - head loss across the valve is
increased or decreased by opening or closing a valve on the
discharge side of the pump; a continuous control technique.
b. Sizes and length of hoses - excess or undersized hosing can
alter total friction head and cause flow changes; system
must be shutoff and drained. Should be performed on dis-
charge side of pump only.
c. Chanaes in static head - changing the location of the re-
ceiving water level with respect to the pumping water level;
(changing the location of the pump alone will not effect a
static head change). System would be shutoff for this change.
3. Bypass systems - Flow control may be achieved by bypassing some
of the fluid from the discharge side of the pump either back to
the suction side or back to the pumping water body. This can
be done without any valves through controlling relative sizes of
378
-------
flow and bypass lines (not a continuous control technique) or
a bypass valve may be installed for continuous flow control.
7.A.2.1 Valves (see Reference 62) - Valve function, more than any other
single criterion limits the choice of valves. For purposes of discussion,
valves may be categorized Into three groupings: on-off service, throttling
service, and prevention of backflow. Pressure drop through valves can be
substantial and so a valve selection which minimizes pressure drop while
still meeting other requirements is obviously best. Valves are available in
a variety of materials of construction to be compatible with corrosive
environments. Materials of construction, however, are sometimes limited to
certain sizes. For example, In water service, valves up to 10 cm (V) size
are generally available in brass or bronze, whereas in sizes above 10 cm
(V) Iron and steel bodies are usually available. Small sizes, up to about
5 cm (2") are screwed and the larger sizes flanged.
Care must also be taken in choosing valves for field treatment processes
to select a valve which will not clog easily from debris. Few field
processes are free of materials which can clog valves and disrupt system
flow.
Varieties of the valve groupings are described below:
1. On-Off Service - Gate, plug, ball, and butterfly valves; gate
valves are the most readily available; full port valves are
best suited for field treatment processes; plug and ball valves
come in venturi and reduced port designs which have increased
pressure losses and susceptabi1ity to clogging; not generally good
for throttling because the valve is almost closed before pressure
begins to rise; in the almost closed position the full port
feature is useless. Butterfly valves, good for on-^ff or
throttling service, are described in the next section.
2. Throttling Service -
a. Globe valve - unidirectional valve; high pressure drop due
to tortuous flow path; Y-pattern and angle-pattern help to
minimize pressure loss;
b. Butterfly valve - built like a stovepipe damper; screwed
pipe connections on small sizes (up to 2 Inch), wafer
design on larger sizes requires mounting between two
flanges; low pressure loss; especially well-suited for
large flows; quite suitable for slurries or solids-bearing
liquids; fast acting;
c. Diaphragm valve - most commonly available In weir pattern;
pressure drop roughly equivalent to globe valve; no packing
required because of complete fluid isolation; excellent for
viscous media, slurries, and corrosive fluids.
379
-------
3. Check Valves - prevent reverse flow tn fluid line; automatic In
operation; are kept open by the pressure of the flowing fluid;
available in swing, tilting disc, lift, or stop-check designs'
of the four varieties, swing and tilting disk have the straight
flow pattern and lowest pressure loss.
7.4.2.2 Flow Splitting - Because of limited availability of valves and the
need to divide flow from a single pump discharge into a number of parallel
treatment processes, a flow splitter is required such as is shown schemat-
ically below.
2-
i 1
1 * 1 TANK 1
D_
1 1
il
_J TANK 2
_J TANK 3
1 TANK k
The flow splitter is basically a plumbing manifold with a single Inlet
and multiple outlets. It can be constructed from either screwed plumbing
fittings or as a weldment. Below are listed some criteria to be used when
designing a flow splitter:
1. Make the fitting as symmetrical as possible from inlet to outlet
without making one flow path easier than another.
OUT
OUT
»OUT
IN
IN
IN
e.g. for the two, three and four outlet manifolds shown above
all flow lines from in to out Involve the same number of bends.
2. Make the total length of the manifold as short as possible.
390
-------
DESIRABLE
b.
UNDESIRABLE
3. The total area of outlet should be less than the manifold area.
man
r
out,
out.
out.
TTD
(D
out
or, generally
D2 > D
man
>2, to2 )
out, out.
out
Note; The manifold area may be enlarged above the Inlet area to meet
this requirement.
A. Do not support heavy manifolds from a pump body. A length of
lead hose to a manifold lying on the ground is preferred.
If the flow splitter does not provide as equal a division of flow as In
desired without the use of valves, some further flow equalizing techniques
may be employed:
1. Varying the discharge elevations of the outlets.
2. Using the longer discharge hoses on the higher flowing lines.
3. Crimping a hose to cause flow restriction, e.g. using a C-clamp
valve as shown below in an end view.
381
-------
WOODEN
BLOCKS
7.5 CHEMICAL FEED COMPONENTS
7.5.) General
Equipment which Is necessary to safely handle the treatment chemicals is
considered separately In two subsections. These chemicals are unsafe to
handle using Improvised systems due to their high concentrations and
corrosive properties. Therefore, specialty equipment manufactured specifi-
cally for handling of these chemicals must be obtained locally by the OSC
and transported to the treatment site.
The descriptions which follow are intended to provide a basic understand-
ing of the types of available chemical feed pumps, tubing fittings and
mixers. This type of equipment is usually handled by suppliers who have
ready access to information from which the best equipment for the particu-
lar application may be selected. To contact suppliers for a local area,
the Yellow Pages should be consul ted under the following, or similar sub-
jects :
Hose and Tubing - Rubber and Plastic
Laboratory Equipment and Supplies
Mixing and Agitation Machinery
Pumps
Tanks -Fiber Glass, Plastic, etc.
Tube Fittings
Tubing - Metal
382
-------
Since the suppliers have the needed expertise, no attempt has been made to
specify the best components for a certain chemical. This specification may
limit the OSC to a certain suitable but unavailable type of equipment, and
thereby halt the treatment operation. Instead, a list of information need-
ed to establish the-suitable equipment type has been presented, (see Figure
75) To use this approach, the OSC should complete the charts and then
relay this information to the supplier. Then the supplier can recommend
the equipment needed.
7.5.2 Chemical Metering Pumps
Chemical feed pumps are normally available at pump supply houses. To
facilitate selection of chemical feed pumps, available pumps are classi-
fied into the following three general headings. These headings differ-
entiate between the different pumping actions and permit identification
of wetted parts which is important when selecting proper materials of
construction. The classification designating A-C are used in other parts
of the manual when referring to these pumps:
Type A. Centrifugal, positive pressure, and gear pumps: Type A
pumps are not positive displacement pumps which means that pumping
volume is not independent of pressure. Thus they are not normally
used where exact metering is critical under all conditions. For
most applications though, where pressure does not fluctuate dramati-
cally, reasonably accurate calibrations can be achieved.
The centrifugal or gear pumps are suitable for pumping chemical
solutions at higher flow rates (typically 3-7 - 170 1pm (l-l»5 gpm))
and low to medium pressures (typically up to 1.3 atm (20 psl). They
are not self-priming and should be operated with a flooded suction.
The positive pressure pumps are capable of pulling suction lifts of
0.9-48 m (3-15 ft) dry and 6.1 - 7.6 m (20-25 ft) primed. They also are
suitable for higher flows (typically 3.7~98 1pm (1-26 gpm)) and low to
medium pressures (typically up to 3.4 atm (50 psi).
They have impellers or gears which rotate at constant or variable
speed. The impellers may be rigid members rotating with a clearance
within the pumping chamber; they may be gears or lobes which mechani-
cally mesh; or they may be flexible impellers which have contact with
the pumping chamber as they rotate. The pumps are either direct
drive, in which case there is a seal around the drive shaft to pre-
vent corrosion of the motor, or magnetically coupled, in which the
drive end is completely independent of the fluid end and no shaft
seal is necessary. Typical materials of construction for the wetted
parts of Type A pumps are listed In Table ^0.
Type B. Reciprocating, Positive Displacement Pumps: These pumps
are capable of producing a fixed or variably controlled output flow
irrespective of system pressure. They are most accurate with a
flooded suction and high pressure outlet (typically 40 psi). In low
pressure systems this outlet pressure can be created artificially
with a backpressure valve.
383
-------
Required information for Establishing Suitable Chemical Feed Equipment
Pumps
1. What is the required flow rate?
2. What chemicals and concentrations are to be
pumped*
Chemicals Concentrations
* One chemical may be pumped at various concentrations so
specify both.
3. What suction lift is required (See 7.2.0?
k. What discharge head is required (See 7.2.l)?_
5- Is flow adjustment needed during operation?
6. At what temperatures will the pump operate?
7. What electrical requirements exist?
Voltage S7ln9le
a 3 phase
Tub i n g a n d F i 11 i ngis
1. What sizes are needed (Tube O.D.)?
2. What will be the operating pressure?
3. What materials and concentrations are to
be pumped? (See pump section)
k. What are the thread specifications for
connected parts?
e.g. nominal size of NPT pipe, threads,
male or female threads, etc.
Figure 75 Information needed to obtain suitable chemical
feed equipment
38k
-------
Tanks
1. What volume is needed?
2. What materials and concentrations are to
be contained?
3- What mixer mount is needed?
side, center, other
k. Where are fittings to be located and what
size is needed?
5. Is the tank to be covered?
Mixers
1. What materials and concentrations are to be mixed?
2. How long will the mixer operate per batch?
3- How many batches will be mixed per day?
^4. What is the tank volume and dimensions?
5. What type of mixing is required?
Rapid mix
Gentle mix
6. What electrical hookups are available?
Voltage Single
3 phase
Figure 75 (continued). Information needed to obtain
suitable chemical feed equipment
385
-------
TABLE 40. MATERIALS OF CONSTRUCTION FOR TYPE A PUMPS
Body
Impeller
Shaft
Seal
Centrifugal (Capacities 25-170 1pm (6.6-45 qpm), maximum pressure
.2-1.5 kg/cm2 (4-21 psl)
polyethylene
nylon
stainless steel
polypropylene
Buna N
Pen ton
polyethylene
stainless steel
polypropylene
Buna N
Penton
stainless steel
nitrile coated
steel
Positive Pressure (Capacities 11-98 1pm (3-26 gpm)
bronze
stainless steel
phenolic
epoxy
nitrile
neoprene
vi ton
epoxy
Buna N
stainless steel
Hastelloy "B"
and "C"
Titanium
Buna N and stain-
less steel
Buna N
Carbon or
none required
for magnetic
drive
neoprene
Buna N
Carbon £ stain-
less
Nitrile
Viton or none
requi red
Gear
stainless steel
delrin plastic
stainless steel stainless steel
teflon
neoprene or
none required
By utilizing micrometer-adjusted mechanical and hydraulic control
linkages, these pumps are capable of accurately metering fluids
from high flows down to a fraction of a gph. They can also pump
against very high pressures.
There are two basic types of positive displacement pumps - plunger
pumps and diaphragm pumps. It is only important here to note that
they represent differences in the types of wetted parts: the plunger
pump with a piston and packed seal and the diaphragm pump with a
flexible displacement element. Both pumps require inlet and outlet
check valves to allow the fluid to be pumped. Typical materials of
construction for the two types of pumps are as follows: (Table 41)
Type C. Peristaltic and Flextble-stator, eccentric-rotor pumps;
pumps employ a squeegee action to pump the fluid.They are thus
These
i i • - t ~~1~~ — — ^ — — — __.—.. •_ •_• p- _...^ « T TV • • w m w * || i^* j mtK b I tU 9 DOS I *"
tlve pressure, rather than positive displacement pumps. They differ
from Type A pumps because there Is no Impeller In the fluid stream.
Rather the rotational action Is transmitted into a progressive squeezing
on either a tube section or a flexible liner within the pump head.
The peristaltic or tube-squeezing pump Is utilized for flow metering
386
-------
TABLE 41. MATERIALS OF CONSTRUCTION FOR POSITIVE DISPLACEMENT PUMPS
oo
Pump body
steel
iron
stainless
steel
PVC
Alloy 20
Monel
Carpenter 20
Plunger pump
Plunger
stainless
steel
ceramic
monel
Lantern ring
stainless
steel
Allow 20
Hostel loy "C"
PVC
alumina-
ceramic
Diaphragm
pump
Diaphragm
or bellows
elastometer
teflon
polyethylene
Buna N
neoprene
Viton
resistant
steels
Valve Body
steel
stainless
steel
PVC
Allow 20
Hostel loy "C"
monel
Check valves
Ball
stainless
steel
PVC
Hostel loy
"C" to "D"
ceramic
Ball seat
stainless
steel
PVC
Alloy 20
monel
Hostelloy "C"
-------
at flows less than 1 gpm and pressures to 1.7 atm (25 psl) under contin-
uous use. The flexible stator pump has a capacity range of from 1.1 -
15 1pm (Q.3-kQ gpm) at up to 2.A atm (35 psi) continuous pressure. Both
pump types are self-priming and both pumps are susceptible to tube or
liner failure after extended use.
The wetted parts used in typical Type C pumps are listed as follows:
Flexible
Pump body Peristaltic tubing stator 1iner
polyethylene tygon gum ribber
teflon viton Buna N
bakelite silicone neoprene
stainless steel hypalon
butyl
vtton
7.5.3 Thermoplastic Tubing and Fittings
Thermoplastic tubing and fittings are perhaps the most versatile for field
hookups of chemical feed systems, particularly because of their flexibility
and ease of assembly. They are suitable for use with a wide range of
chemicals. Typical sizes and ratings are given in Table 42.
Thermoplastic fittings can also connect tubing constructed of the following
materials: copper, brass, steel, stainless steel, glass, plastic, aluminum.
7.5.3.1 Thermoplastic Insert Fittings - Polyethylene or nylon shank fittings
(require clamps) can be used with either reinforced or non-reinforced cbsar
vinyl plastic hosing or rubber hosing in the 0.5-5 cm (3/16 - 2 in.) inside
diameter range and at working pressures up to 8.5 atm (125 psi). Clear
vinyl tubing and hosing can be obtained in a variety of wall thickenesses for
use with these insert fittings, providing a wide range of pressure ratings.
7;5.3.2 Metal Tubing and Fittings - Metal tubing fittings are available In
brass, stainless steel, steel, and aluminum typically in sizes from 0.17 -
2.5 cm (1/16 - 1 in.) 0.0. They can be used with steel, stainless steel,
copper, aluminum, glass, and plastic tubing. Many types require only wrenches
to install. However, tube cutting and bending devices are desirable when
using metal tubing.
7.5.4 Chemical Feed Tanks
Several varieties of polyethylene and fiberglass tanks are available out
of stock from the manufacturers. The most readily available are flat bottom,
open top tanks in the 0.23-1.7 cu m (60-450 gal.) range. Also available but
probably not from stock are dished bottom, open top tanks, with bottom
fittings to accommodate filling and emptying. Concrete tanks, such as septic
tanks or tanks constructed from sewer tiles as described in Section 7.3.3 can
also be used to mix and store chemicals.
388
-------
TABLE *2. TYPICAL THERMOPLASTIC TUBE SIZE
polypropylene
nylon
vinyl (clear)
(formula PV-1
polyethylene
Pressure
rating,
psi
(rigid) 190
250
250
65
or PV-2) 55
*5
30
120
1*5
125
90
70
Lengths, Outs
ft
10
500
250
50
50
50
50
1000
500
500
250
3/8,
1/8,
I/*,
1
I/*
5/16
1/2
5/8
I/*
5/16
3/8
1/2
ide diameter,
in.
1/2, 5/8
3/16
5/16, 3/8,
/2
, 3/8
100-500 5/8
Fittings - nylon and polypropylene
pressure
ratings - Tube O.D.
I/*
5/16
3/8
1/2
5/8
Working
up to 75
300
300
250
200
150
Temperature,
76-125
300
300
250
200
100
F
126-175
300
300
150
150
50
available fittings: unions, connectors for tubing to male or female
pipe threads, tees, reducer unions, elbows
psi x .068 - atm
feet x 0.305 = m
meters x 2.5* - cm
(°F - 32) x 5/9 - °C.
389
-------
7.5.5 Chemical Feed Mixers
Impeller mixers, both direct drive and gear drive are available, although
the gear drive operating at about 350 rpm is more suitable for chemical
mixing. The shaft length and number and configuration of impellers must
be based on the geometry of the chemical tank. Portable mixers are usually
equipped with clamp mounts and ball and socket index positioning joints.
Stainless steel, Type 316, shaft and impellers are typically used on
chemical service, with rubber covering used on some severe corrosives such
as ferric chloride.
Power requirements range from .18 - 2.2 kw (1/4 - 3 HP) are available and
the following preliminary sizings are presented for reference:
1. For dissolving chemicals and mixing acfds and bases - .25 kw for
1,893 i, tank, and .56 kw for a 3,785 * tank (1/3 hp for 500 gallon
tank, 3/4 hp for 1000 gallon tank).
2. For mixing polyelectrolytes or lime - .56 kw for a 1,893 !• and 1.2
kw for a 3,785 i tank (3/4 hp for 500 gallon tank, 1 1/2 hp for
1000 gal Ion tank.
7.6 AIR COMPRESSORS AND BLOWERS
The typical uses for air in field implemented treatment operations are for
use on air driven diaphragm pumps and for aeration. The most readily
available compressor is the rotary screw compressor, which is a constant
volume device, capable of pressure control down to 4 atm (60 psi). In
applications such as aeration where pressures less than .34 atm (5 psi) are
required, an additional pressure regulator and flow bypass valve will be
needed to provide flow control. Table 43 summarizes potential sources of
air compressors and blowers.
7.7 SELECTION OF CORROSION RESISTANT MATERIALS OF CONSTRUCTION
This subsection provides information on the various materials of construc-
tion which are available. Included is information regarding trade names,
corrosion resistances and typical uses of both ferrous and non-ferrous
metals and other nonmetallic materials. The general corrosion resistance
properties are discussed. In most spill situations, the flow stream will
contain only diluted contaminants so corrosion problems will be minimal.
The most corrosive materials are the treatment chemicals and special types
of chemical feed pumps and components must be obtained. It Is recommended
that the user contact the manufacturers of various equipment, detail the
specific conditions of the contaminated water and treatment chemicals and
then choose the type of materials needed. This section will then allow the
user to augment his knowledge of the materials involved and check the
recommended application. The material presented is summarized in most part
from "Corrosion Engineering" written by M. G. Fontana and N. D. Green (63).
Further information regarding materials is available in this text and other
references.
390
-------
7.7.1 Metals
1. gast i ron - This material is found in many cast process com-
ponents such as pump bodies, impellers, valve parts, etc. Cast
iron is a general term applied to high carbon-iron alloys con-
taining silicon. Common varieties are: gray, white, malleable,
ductile, and nodular. The material is quite susceptible to
oxidation or "rust".
Increasing the silicon content to over \k% produces an extremely
corrosion resistant material, te.g. Duriron, which is very hard
and resists erosion-corrosion (notable exception: hydrofluoric
TABLE A3. SOURCES AND SIZES OF AIR COMPRESSORS
Air Compressors:
Sources
Contractor
Supply House
S ize
150-650
scfm
Pressures
100-125 psig
Comments
Low capacity are gas
engine powered and
higher capacity are
diesel engine powered.
Requi re pressure
regulators to give
lower delivery
pressures, Can normally
be rented.
Local Sewage
Treatment
Plant
Local DPW
Fire Dept.
Manufacturers
of Blowers
150-650
scfm
150-650
scfm
150-650
scfm
Wide range
of sizes
100-125 psig
100-125 psig
100-125 psig
Low pressure Generally must be
up to 15 psi purchased.
scfm x .028 = scum/min.
psi x .068 = atm
391
-------
acid). The alloy is sometimes modified by the addition of 3%
molybdenum, e.g. Durichlor or Durichlor 51, for increased resis-
tance to hydrochloric acid and chlorides.
In addition to alloys using silicon and molybdenum, other alloys
using nickel, chromium and copper also produce improved corro-
sion resistance. Copper addition causes the metal to better
withstand attack from sulfuric acid. High nickel-chromiurn cast
irons with and without copper, e.g. Ni-Resist and Ni-Hard, pro-
duce very tough castings to resist erosion-corrosion in near-
neutral and alkaline solutions or slurries.
2. Carbon steel - Carbon steel is alloyed, in various combinations,
with chromium, nickel, copper, molybdenum, phosphorous, and
vanadium. Low-alloy steels (2% total maximum alloying elements
or less) are generally the more corrosion resistant. However,
like cast iron, it is very susceptible to rusting.
Steel products are cast and also readily available in sheet,
plate, and structural forms, as well as in a variety of products.
Steels can be easily field cut and welded.
3. Stainless Steel - Stainless steel has the same versatility of usage
as carbon steel, with greatly improved corrosion resistance.
Desired corrosion resistant properties are produced by alloying
at least 11 percent of chromium. The chromium is reactive, but
sets up a passive film to inhibit further corrosion.
The following (6*») is a brief description of the five types of cor-
rosion resistant alloys most commonly used in chemical applica-
tions :
Type 304 The basic 18% Cr-8% Ni type for relatively
mild corrosion resistance.
Type 316 The "18-8" type with 2.0/3.0% Mo for superior
resistance to pitting and to most types of
corrosion, particularly in reducing and neutral
solutions.
Type 317 The "18-8" type with 3.0/4.0* Mo, which has
moderately better resistance than type 316
in some conditions, such as high concentra-
tions of acetic anhydride and hot acetic acid.
"20" A 23% Ni-20% Cr steel with copper and molyb-
denum, developed specifically for resistance
to sulfuric acid.
Ni-o-nel A k2% Ni-21.5% Cr alloy with copper and
molybdenum, developed to meet more severe
corrosion and stress-corrosion conditions than
can be handled by the stainless steels but
where nickel-base alloys are not needed.
392
-------
k. Aluminum and Alloys - Next to carbon steel and stainless steel,
aluminum represents a versatile metal for construction, available
in cast form and sheet, plate, and structural forms and in a
variety of commercially available process components.
Aluminum is reactive but develops a passive oxide film which
protects it from further corrosion in many environments. This
film remains stable in neutral and many acid solutions, but is
attacked by alkalies. The passive film is produced after contact
with the chemical environment, unless the film has been artificial-
ly produced through anodizing. Structural members are typically
produced from high-copper alloys, whereas process components are
usually constructed of the low-copper or copper-free alloys, which
have better corrosion resistance.
5« Magnesium and Alloys - A lightweight material often found on
portable devices and vehicles, however one of the least corrosion
resistant. It must generally be physically separated from other
metals or it will become a sacrificial anode for them. It is
capable of forming a good passive film, however, the film breaks
down in salty air conditions, necessitating that special coatings
or other surface preparations be used. Magnesium is susceptible
to erosion-corrosion. It is much more resistant to alkalies
than is aluminum. It is attacked by most acids except chromic
and hydrofluoric. The corrosion product in HF acts as a protec-
tive f i 1m.
6. Lead and Alloys - Used often on corrosion resistant applications
in such forms as : sheet linings, solder, cable sheath, bearings,
and piping. Lead forms protective films consisting of corrosion
products such as sulfates, oxides, and phosphates. It is subject
to erosion-corrosion because of its softness. Chemical-resistant
lead, containing about 0.06% copper, is resistant to sulfuric,
chromic, hydrofluoric, and phosphoric acids, neutral solutions,
and seawater. It is rapidly attacked by acetic acid and generally
not used In nitric, hydrochloric, and organic acids.
7. Copper and Alloys - Copper alloys are found in pump bodies and
Impe11ers, process component bodies and parts, and in pipe tubing
and fittings, tanks, bearings, wire and screen.
A good chemically resistant material, copper is a noble metal and
is not corroded by acids unless oxygen or other oxidizing agents
(e.g. HNO_) are present. Copper-base alloys are resistant to
neutral and slightly alkaline solutions (exception: ammonia).
Common alloys are: brass, bronze, and cupernickel. Bronze.
aluminum brass, and cupranickel are stronger and harder than copper
and brass and less subject to erosion-corrosion.
8. Nickel and Alloys - A workhorse in severe corrosion applications,
n i ckel and i ts alloys are found in many commercially available
393
-------
process components, especially pumps, valve parts, and other
critical process parts. Nickel is resistant to many corrosives
and is a natural for alkaline solutions, found in many tough
applications on caustics. It shows good resistance to neutral
and slightly acid solutions. It is not resistant to strongly
oxidizing solutions, e.g. nitric acid, ammonia. Among the
common varieties:
Monel - natural for hydrofluoric acid
Chlorimet 3 and Haste Hoy C - two of the most
generally corrosion-res is tant materials com-
mercial ly available
Chlorimet 2 and Hastelloy B - very good in cases
where oxidizing conditions do not exist
9. Zinc and Alloys - Not a corrosion-resistant metal, chiefly used
in galvanized steel.
10. Tin and Tin Plate - Usually found as a coating and is used in
solder and babbit bearings, is corrosion resistant, easily formed
and soldered; and provides a good base for organic coatings. Tin
has good resistance to dilute mineral acids in the absence of air,
and many organic acids, but is corroded by strong organic acids;
generally not used for handling alkalies.
11. Titanium and Alloys - A newcomer to corrosion resistant construc-
tion, is available as castings in pumps, valves, and other process
components. Titanium is a reactive metal which depends on a pas-
sive oxide film for corrosion resistance. Titanium has resistance
to seawater and other chloride salt solution; hypochlorites and
wet chlorine; and nitric acid. Salts such as Fed- and CuCl2»
which tend to pit other metals do not corrode titanium. It is
not resistant to relatively pure sulfuric and hydrochloric acids.
7.7.2 Nonmetal1ics
1. Natural and Synthetic Rubbers - Rubber is an important process
material with an extensive range of uses: hoses, tanks, tubing,
gaskets, pump diaphragms and impellers, sheets, liners, etc.
Rubber has excellent chemical resistance, and has been a standard
for handling of hydrochloric acid. Generally, the synthetic
rubbers have better chemical resistance than the natural rubbers.
Vulcanization, the process of hardening rubber by adding sulfur
and heating, can produce a wide range of hardnesses from soft
gaskets to hard pump impellers. Corrosion resistance generally
increases with hardness.
A wide variety of synthetic rubbers is available, including com-
binations with plastics. In developing the various products,
39A
-------
plastlcfzer fillers and hardeners are compounded to obtain a
large range of properties, Including chemical resistance.
Table V» shows chemical resistance and other properties of
commercially available rubber products. One of the newer elas-
tomers which should be added to the list Is Hypalon, which has
excellent resistance to oxidizing environments such as 30%
sulfurlc acid and 1*0% nitric acid at room temperature.
Plastics - Used extensively In chemical process applications as
process component bodies and parts, tanks and tank liners, pipe,
valves, tubing, and fittings, sheets, structurals, etc., plastics
are high-molecular weight organic materials that can be shaped
into a variety of useful forms.
When comparing plastics to metals, the former are softer and
weaker, more resistant to chloride ions and hydrochloric acid,
less resistant to concentrated sulfurlc and oxidizing acids such
as nitric, less resistant to solvents, and have definitely lower
temperature limitations.
Plastics, when subjected to corrosive environments do not fail
as metals do. Rather than dissolving, they are degraded or
corroded because of swelling, loss in mechanical properties,
softening, hardening, spall ing, and discoloration. Table ^5
lists the properties of some commercially available plastics.
For ease of using this table, commonly used tradenames and other
designations are listed here alphabetically In reference to the
chart classification to which they belong:
Material Chart Classification
Aeroflex Polyethylene
Alathon Polyethylene
Araldite Epoxy
Avisco Urea
Bakelite Phenolic
Beelte Urea
Dacron Polyester
Durcon Epoxy
Durez Phenolic
Dypol Polyester
Epon Epoxy
Excon Polypropylene
Kel F Fluorocarbon
Lauxite Urea
Lucite Methyl methacrylate
Lustrex Polystyrene
Moplen Polypropylene
395
-------
TABLE kk. PROPERTY COMPARISONS - NATURAL AND SYNTHETIC RUBBERS (63)
Property
Hardness range (Shore "A") a
Tensile strength, psi fc
Max. elongation, %
Abrasion resistance c
Resistance to compression set
at 158°F c
Resistance to compression set
up to 2500F c
Aging resistance (normal temp.)
Max. ambient temp, allowable, °F
Resistance to weather and ozone c
Resistance to flexing
Resistance to diffusion of gases
Resi 1 ience
Resistance to petroleum oils
and greases
Resistance to vegetable oils
Resistance to non-aromatic
fuels and solvents
Resistance to aromatic fuels
and solvents
Resistance to water and
anti-freezes c
Resistance to dilute acids
Resistance to oxidizing agents
Resistance to alkal I
Dielectric strength c
Flame resistance
Processing characteristics
Low temp, resistance c
Tear resistance
Natural
rubber
1(0-100
1(500
900
Excel lent
Good
Poor
Good
160
Fair
Excel lent
Fair
Excel lent
Poor
Good
Poor
Poor
Good
Good
Poor
Fair
Excel lent
Poor
Excel lent
Ve ry good
Excel lent
Butyl
(GR-I)
i(0-9o
3000
900
Good
Fair
Poor
Excel lent
275
Very good
Excel lent
Excel lent
Poor at
1 ow temp .
Good at
high temp.
Poor
Good
Poor
Poor
Good
Good
Fair
Fair
Good
Poor
Good
Fai r
Excel lent
Buna S
(GR-S)
1(0-100
3500
600
Excel lent
Excel lent
Excel lent
Excel lent
275
Fair
Good
Fair
Fair
Poor
Poor
Poor
Good
Good
Poor
Fai r
Excel lent
Poor
Good
Good
Good
Neoprene
30-90
3500
1000
Very good
Good
Fair
Excel lent
225
Excel lent
Exce 1 1 en t
Very good
Very good
Good
Fai r to
good
Fair
Fair
Good
Poor
Good
Fair
Good
Good
Fair
Good
Nitrl le
(buna N)
1(5-100
1(000
700
Excel lent
Excel lent
Excel lent
Excel lent
300
Fair
Fair
Fai r
Fair
Excel lent
Very Good
Good
Excel lent
Good
Poor
Fair
Fair
Poor
Good
Good
Good
Polyacryl ic
rubber
50-30
1500
200
Fair
Good
Good
Excel lent
1»00
Excel lent
Excel lent
Poor
Very good
Poor
Fair
Poor
Fair
SI 11 cone
rubber
1«0-80
900
250
Poor
Excel lent
Excellent
Excel lent
580
Excel lent
Poor
Good
Fair
Poor
Fair
Poor
Excel lent
Poor
a 100 Durometer reading Is bone hard and indicates that ebonite or hard rubber can be made.
t Indicates soft-rubber type. Hard-rubber types run higher In value.
c These properties available In specific compounds.
-------
TABLE
PROPERTIES OF COMMERCIALLY AVAILABLE PLASTICS (63)
vo
Acids
Material
Weak
Strong
Alkalies
Weak
Strong
Organ ic
solvents
Water Oxygen
absorption, and
1/2*4 hr ozone
1 on I 2 1 n g
High aadla-
vacuum tion
Temperature
Resistance
High
Low
Thermoplastics
Fluorocarbons
Methyl methacrylate
Nylon
Polyether (chlorinated)
Polyethylene (low density)
Polyethylene (high density)
Polypropylene
Polystyrene
Rigid polyvinyl chloride
Vinyls (chloride)
inert
R
G
R
R
R
R
R
R
R
inert
A-0
A
A-0
A-0
A-0
A-0
A-0
R
R
Inert
R
R
R
R
R
R
R
R
R
inert
A
R
R
R
R
R
R
R
R
Inert
A
R
G
G
G
R
A
A
A
0.0
0.2
1.5
0.01
0.15
0.1
<0.01
0.0't
0.10
O.liS
inert
R
SA
R
A
A
A
SA
R
R
-
decomp.
-
-
F
F
F
P
-
P
P
P
F
-
F
G
G
G
P
P
550
180
300
280
\ko
160
300
160
150
160
G-275
-
G-70
G
G-80
G-100
P
P
P
~
Thermosetters
Epoxy (cast)
Phenol Ics
Polyesters
SI 11 cones
Ureas
R
SA
SA
SA
A
SA
A
A
SA
A
R
SA
A
SA
A
R
A
A
SA
A
G
SA
SA
A
R
0.1
0.6
0.2
0.15
0.6
SA
-
A
R
A
-
-
-
-
G
G
G
F
P
boo
400
350
550
170
L
L
L
L
L
NOTE: R = resistant, A = attacked, SA - slight attack, A-0 - attacked by oxidizing acids, G = good, F - fair, P • poor, L • little change.
-------
Mylar Polyester
Nylon MO"
Pen ton Polyether
Plexlglas Methyl methacrylate
Plloflex Vinyl
Polythene Polyethylene
Pro-Fax Polypropylene
pvc Polyvinyl chloride
Resinox Phenolic
Saran V^Y1
Styron Polystyrene
Teflon Fluorocarbon
Tygon
Vibrin Polyester
Vinylite
Viton Fluorocarbon
3. Other Nonmetal 1 i cs - Used as materials of construction and
lining of process systems:
Ceramics - compounds of metallic and non-metallic elements;
include magnesia, brick, stone, fused silica, stone-
ware, glass, clay tile, porcelain, concrete, abrasives,
mortar, high temperature refractories. Most ceramics
exhibit good chemical resistance, with the exception
of hydrofluoric acid and caustic.
Carbon and Graphite - often used for shaft seals; inert to many
chemical environments; good resistance to alkalies
and most acids; attacked by oxidizing acids such as
nitric, concentrated sulfuric, and chromic; also
attacked by fluorine, iodine, bromine, chlorine, and
chlorine dioxide.
Wood - Typical chemically resistant woods are cypress, pine,
oak, and redwood; generally limited to dilute chemi-
cals; strong acids, oxidizing acids, and dilute
alkalies attack wood.
7-7-3 Protective Coatings
Paints, varnishes, lacquers, and similar coatings are capable of prevent-
ing corrosive attack of the substrate material when they are properly
selected and correctly applied. Three main areas of concern are surface
preparation, and selection of primer and top coat.
1. Surface preparation - involves removal of dirt, rust, mill scale,
oil, grease, and other impurities. Surface should be roughened
to give a good mechanical bond. Cleaning techniques include
scrubbing, wire brushing, sanding, chipping, hole filling, torch-
ing, solvent cleaning, etc.
398
-------
2. Primers - can contain rust-lnhibitlve pigments such as zinc
chromate and zinc dust; short drying time paints can expedite
field application of top coat.
3- Top coats - vinyl and epoxy paints are commonly used for corrosion
applications; many other varieties are also available.
7.8 INFORMATION ON TREATMENT CHEMICALS
7.8.1 General
This section details Information on various chemicals which can be used
to treat the hazardous spilled materials. Many of the chemicals recom-
mended for use are in themselves very hazardous and must be handled with
caution. Two subsections are included. The first deals with the vari-
ous calculations necessary when chemicals are being handled. The steps
include scaleups from bench testing values to ordering the necessary
amounts of chemicals to diluting the concentrated chemicals to feed
concentrations. The calculations are outlined in this portion of the
manual. The second subsection includes additional Information on each
of the specific chemicals. The information included is as specific as
possible but the manufacturer or supplier should be requested to send
additional detailed Information with the shipped material.
7.8.2 Calculations for Chemical Ordering and Mixing
7.8.2^1 General * The following calculations are designed to allow
ordering and mixing of chemicals for the treatment processes. These
calculations yield the minimum amounts to order. It Is suggested that
a 25% excess over the calculated value be ordered to prevent chemical
shortages from varying waste quality and chemical spillage, etc.
Frequently, unused and unopened containers of chemicals can be returned
to the supplier. Chemicals should be ordered as soon as possible to
insure arrival on site when the treatment facilities are completed.
7-8.2.2 Conversion of bench scale results to mg/ml - When conducting
bench scale te"sts it is nece^sar*y to ekpfesJT tTte bptlmum chemical
dosage as a weight to volume ratio so that the results can be applied
to ordering and mixing chemicals.
Solution: (Bench test chemical cone, mg/ml) x (mis added)=
mis of sample treated
mg bench test chemical
ml of sample
jExample: What Is the mg of NaOH required per ml of sample for the
following test results?
Volume of sample tested: 500 ml
Amount of NaOH added: 25 ml
399
-------
7.8.2 Mixing chemical to desired strength - After receiving the
t rea'ttne n't chem i ca 1 s i t usually is necessary to dilute them to an acceptable
concentration for addition.
Solution: If chemical is in the dry form its weight will be known. If
it comes as a liquid it can be converted to a weight as
fol lows:
Metric: kg of chemical = I of chemical x density (g/l) x 10
English: Ibs of chemical = (gallons of chemical) (8.3*0 (Specific
gravity of chemical)
Knowing the desired chemical feed concentration the gallons of water
needed per pound of chemical can be determined as follows:
gal Ions of water needed _ % purity
Ib of chemical % feed concentration
Example^; Determine the amount of water needed to mix 20 pounds of
NaOH into a 5% solution.
gallons of water needed
"
Ib of cfiemical 5 x 8.34
Total amount of water needed = (2.25 gallons) (20 Ib) =
Ib
kS gallons.
gal. x 3-785 = 1
Ib x .454 - kg
Solution^ If- a known amount of dilution water is to be used and the
desired feed concentration is known, the amount of chemical
to be added can be calculated as follows:
Ibs of chemical = % feed concentration x 8.33
gallon of water = '(% purity)
Examp 1 e : Determine the amount of NaOH at 94% purity needed to mix
100 gallons of a 5% NaOH solution.
Ibs of chemical 5 x 8.3*1 . ,
gallon of water =~79?J =
Total pounds required » (0.44 Ibs ) (100 gal.) = Mf.Albs.
gal.
gal. x 3-785 = 1
Ib. x .*»5A - kg
400
-------
7.8.2.5 Ordering liquid chemicals - The purity of certain treatment
chemicals ts often expressed in degrees baume (Be'"). By asking the
supplier or referring to a chemical handbook the concentration of the
chemical itself can be determined. The normality of the solution
should also be known. Listed below are some of the concentrations of
chemicals used in treatment.
Chemi cal
Acetic acid
Acetic acid
Hydrochloric acid
Sulfuric acid
* by
weight
96
99-100
36
95-97
Density
020°
ko
1.06
1.06
1.18
1.84
Baume '
degrees
8
8
22
66
Approximate
normal i ty
17
18
12
36
If the results from bench scale tests are reported in mis needed per ml
of liquid to be treated, it is possible to calculate the amount of
chemical needed as follows:
Solution: Gallons of chemical required =»
(mis used) (Normally used in lab tests) x (Gallons to be treated)
(mis of sample)(Normality of chemical
ordered)
Example: How much 66° Baume' 3&N sulfuric acid is required to
treat 1,000,000 gallons if bench scale tests using 2N
sulfuric showed that 25 ml were needed for each 500 ml
to be treated?
Gallons of chemical required = (25) (2N) (1,000,000)- 277R gal.
(55o)l35M)
gal. x 3-785 = 1
If the chemical ordered is based on bench scale tests expressed in mg/1
the amount of chemical needed can be determined.
Solution: Knowing the % by weight and the density of the solution,
the concentration of the chemical itself can be calcu-
lated as follows:
Concentration of chemical =
in Ib/gallon
(Density of - % by weight
solution - ^ * of solution)
The number of pounds required is simply determined as follows
401
-------
Concentration of MaOH test solution: 100 mg/ml
(100 mg/ml NaOH) x (25 ml) = 2500 mg/ml r , . .. nu
- ml samp,e - 500-^ - " 5 mg/ml NaOH
7^.8.2.3 Calculating the total amount of chemical to order - Using the
previous example, the total of amount of chemical required can be
determined:
Solution: kg needed = ^liters to treat) (mg/ml dosage)
~% purity of chemical 0.00834
Ibs. needed » (gallons to treat)^ (mg/ml dosage) x 0.834
% purity of chemical
Exampjej How much 94% pure NaOH is needed to treat a spill of
100,000 gallons?
NaOH dosage = 5 mg/ml
gallons to treat » 100,000
NaOH purity - 94%
The following metric conversions are appropriate:
gal. x 3.785 - 1
Ib x 0.454 - kg
Ibs needed = (100,000) x (5) x 0.834
-- jp. --
If coagulants are used in the bench tests and the desired dosages are
given in mg/1 the pounds required can be determined.
Solution: Ibs needed = (gallons to be treated) (mg/1 coagulant) (8.34)
_
purity x 10,000
*MWR is the Molecular Weight Ratio and represents the molecular weight
of the chemical ordered divided by the molecular weight of the coagulant
itself.
Example: How much Ca(OH) is needed to treat 1,000,000 gallons
based upon a required CaO coagulant dosage of 100 mg/ll
Coagulant dosage = 100 mg/l as CaO
Chemical ordered *= Ca (OH)
% purity =98 2
Gallons to treat = 1,000,000
MW of CaO » 56
MW of Ca(OH)2 = 74
Ibs needed = (1 ,000,000) (100) (8.34) x 74 = ,,,•,,,.
9"8 x 10000 - J5 112/»lbs
402
-------
Example:
Ibs required » (gallons to be treated) (8.3*0 (mg/1)
I ,000,000
Ib x .*»5*t = kg
The number of gallons required is calculated as follows:
Number of gallons = {Ibs required) (concentration of chemical
in Ib/gallon)
gal. x 3.785 = 1
How much FeCl3 is required to treat 100,000 gallons if
bench scale tests showed that 50 mg/1 of FeCl3 ?s the
needed dosage and with a density of 1.^30 and is A0%
FeCl 3 by weight:
Concentration of chemical » (I .^30) (0. 083*0 (z>0) = A. 77 Ib/gal
Ib/gal.
Ibs required = (100,000) (8.3*0 (50)
1,000,000
,.
lb
Number of gallons - (^1.6)7(^.77) = 8.71* gal.
7_.8.2.6 Diluting liquid chemicals - When diluting liquids such as acetic
acid, sulfuric acid or hydrochloric acid for feeding to the treatment
system, concentrations i to i of the original concentrations are usually
used. Since the reaction itself will be monitored (e.g. pH meters) a
precise feed concentration is not necessary, therefore a volume to
volume dilution will be sufficient.
Solution: To determine the amount of dilution water necessary to
reduce the original concentration, the following formula
can be used.
Amount of
water to add
(Original % (Original amount
concentration) x of water)
Desired concentration %
- (Original amount of water)
Example: Determine the amount of water needed to dilute 500
gallons of 93% pure acid to 33%.
Amount of water to be added = (93)(500ga1s)-500ga1s=910gal
33
403
-------
7.8.3 Chem? ca 1 Data Sheets
The following chemical data sheets are provided as guidelines for using
treatment chemicals. Approximate prices are given for estimating purposes,
however, these vary with the purity and quantity of the chemical ordered.
The safety precautions listed are minimal. More specific information
should be obtained from the manufacturer prior to receiving shipment of
chemicals. It is stressed that many of the treatment chemicals are hazard-
ous themselves and must be treated as such. All operators handling chem-
icals should wear goggles and in most cases chemically resistant aprons
and gloves should be used. All chemicals on site should be stored in
an isolated area so that unauthorized personnel will not come in contact
with them. The handling of chemicals on site must eliminate compounding
the hazard that already exists.
Other information also included on the data sheets regards recommended
bench testing and feed concentrations for the chemical. •Special mixing
methods are listed as an aid for those handling the chemical. The cau-
tions reiterate some of the specific problems or hazard potentials.
Finally the materials of construction which are acceptable for using the
chemical are listed. These are general guidelines since the actual
corrosiveness of the solution cannot be estimated and the equipment will
only be used on a short term basis so a small rate of corrosion can be
tolerated.
404
-------
Chemical name: Acetic acid Synonyms:
CH.COOH
Alternate chemicals: Very dilute HCl/vinegar (not desirable).
Common package sizes: k$Q Ib drums.
Approximate costs: $28.00/100 Ib.
Purities (from manufacturer) 99.5% (glacial acetic)
and bulk density:
Bench test concentrations: up to 100%.
End point determinations: pH meter.
Personal safety: Vapors are irritating to eyes, nose and throat/move victim
to fresh air. Compound will burn skin and eyes. Harmful or fatal if
swallowed. Remove contaminated clothing and shoes. Flush with plenty of
water. If swallowed, give water or milk. DO NOT induce vomiting. Avoid
contact with liquid or vapor.
Special mixing methods: Acid to water.
Cautions: Gives off heat upon mixing with water/always add acid to water
or a danger of explosion exists.
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic
Pumps &
Fittings:
kg
Figure 76. Data sheet on Acetic acid,
405
-------
Chemical name: Aluminum sulfate (Alum) Synonyms: Alum
Al_ (SO.) , . 18 H,0 Filter Alum
3 Sulfate of Alumina
Alternate chemicals: Ferric chloride or ferric sulfate.
Common package sizes: 100 Ib bags 250/350 1b barr. bulk C/L
Approximate costs: $5-90/100 Ibs.
Purities (from manufacturer) \7% AKO (alum'num oxide) 60-75#/ft3
and bulk density: *
Bench test concentrations: 100 mg/ml as A12(SO.)_ . 18 H20.
Feed concentrations: 1%
End point determinations: Floe is substantial.
Personal safety: Hazardous if ingested or inhaled - avoid breathing dust.
May form acid solution capable of causing burns. In case of contact with
skin or eyes remove clothing and shoes and flush with plenty of water.
Special mixing methods: Is slow to dissolve so mixing is critical.
Cautions: Granular solid is superior/corrosive and acidic once in solu-
tion. Be careful not to breathe dust.
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic
Pumps & Dry - iron/steel/concrete Wet - lead/rubber/Duriron/
Fittings: asphalt/cypross/3l^-st.
steel
• kg
Figure 77- Data sheet on Aluminum sulfate.
-------
Chemical name: Calcium Chloride Synonyms:
CaCl-
Alternate chemicals: None
Common package sizes: Flakes: 100 Ib bags Pellets: 80 Ib lots
Approximate costs: $7.25 - 11.35/1001 $8.65 - I3.50/I00#
Purities:(from manufacturer): 77-9^% as CaCl_.
Bench test concentrations: 100 mg/ml
Feed concentrations: 10-20%.
End point determinations: When Ca ppt is no longer formed.
Personal safety: Do not inhale or ingest. Remove victim to fresh air.
Remove contaminated clothing and shoes and flush with plenty of w=»ter.
Special mixing methods: Dissolves easily/do not breath dust/heat may be
liberated when dissolved.
Cautions: Is Somewhat corrosive/flakes dissolve quickly.
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic/other
Pumps 6 Cone: Dilute:
Fittings: Rubber Steel (up to 50?: cast iron)
= kg
Figure 7R. Data sheet on Calcium chloride.
407
-------
Chemical name: Calcium Hydroxide- Synonyms: Chemical lime
slaked lime - Ca(OH)2 Lime
Slaked lime
Hydrated lime
Alternate chemicals: Calcium oxide.
Common packages sizes: 50# bag.
Approximate costs: $2.0VlOO#.
Purities (from manufacturer) 9^-95% 35-50 lb/ft3.
and bulk density*
Bench test concentrations: 100 mg/ml as CaO.
Feed concentrations: Dry or 10% solution (0.93 lb/gal.).
End point determinations: pH and floe production.
Personal safety: Dust irritating to nose and throat - move to fresh air.
Will burn skin and eyes. Harmful if swallowed. Remove contaminated
clothing and shoes. Flush affected area with plenty of water. If
swallowed and victim is conscious have victim drink water or milk. D£
NOT induce vomiting.
Special mixing methods: Lime will form a slurry which requires mixing
throughout the feeding period. Slaking of Ca(OH)2 requires 30-60 min to
complete. Use velocities of 5~7 fps to feed.
Cautions: Heats and expands on reaction with water. Adsorbs H£0 and
C02 from air to form CaCO}. Do not breathe dust.
Materials for handling:
Tanks: Process - any
Chemical - plastic/other
Pumps & Rubber hose/iron/steel/asphalt/concrete
Fittings: Mo lead
kg
gal. x 3-785 - 1
Figure 79. Data sheet on Calcium hydroxide.
-------
Chemical name: Calcium oxide (lime) Synonyms: Unslaked lime
CaO Quick lime
Burnt lime
Alternate chemicals: Calcium hydroxide.
Common package sizes: 80 Ib bags.
Approximate costs: $2.28/100 Ib.
Purities (from manufacturer) 9^-95? 55-70 lb/ft3
and bulk density?
Bench test concentrations: 100 mg/ml as CaO.
Feed concentrations: Slake and dilute to less than 10% - Each pound of
CaO will slake to I.16-1.32 Ib of Ca(OH)2 and 2-172 grit.
End point determinations: pH and floe formation.
Personal safety: Dust irritating to nose and throat. Move victim to fresh
air. Will burn and eyes. Harmful if ingested. Remove contaminated
clothing and shoes. Flush affected area with plenty of water. If swallowed
and victim Is conscious, have victim drink water or milk. DO NOT induce
vomiting.
Special mixing methods: Slaking requires 30-60 minutes with heat evolution
and expansion: slurry will require continuous mixing and pumping at 5~7 f ps,
Cautions: Basic and adds alkalinity to water/can be corrosive/will increase
water temperature. Caution is needed.
Materials for handling:
Tanks: Process - any
Chemical - plastic/other
Pumps & Dry - iron/steel/concrete Wet - Iron/steel/rubber
Fittings: hose/concrete
kg
Figure 80. Data sheet on Calcium oxide,
409
-------
Chemical name: Ferric chloride Synonyms: Ferric chloride
Fed, Chloride of iron
Crystal ferric chloride
Anhydrous ferric chloride
Ferric floe
Alternate chemicals: Alum/ferric sulfate
Ferrous sulfate
Common package sizes: 55 gal. drum-42° baume1 175 and 610 Ib drums
Approximate costs: $9-65/100 Ib (liquid)
Purities (from manufacturer): Liquid - 392 - 11.2-l2.4#/ft3
Solid-hepta hydrate 60% FeCl r>-60-6Wft 3
and bulk density J
Bench test concentrations: 100 mg/ml Fed 3.
Feed concentrations: <45% generally, 15% will control hydrolysis.
End point determinations: pH and floe formation.
Personal safety: Forms corrosive acid solution in water. Releases toxic
chlorides when heated to decomposition. Mild irritant. Slight ingestion
hazard. Remove contaminated clothing and shoes and flush with plenty of
water-
Special mixing methods: Dissolves very easily and should be fed in solution.
Cautions: Is a hygroscopic solid and forms an acidic and corrosive liquid/
protect from light.
Materials for handling:
Tasks: Process - any
Chemical - concrete/plastic
Pumps £ Rubber/glass/ceramics/plastic
Fittings:
kg
Figure 8l. Data sheet on Ferric chloride.
-------
Chemical name: Ferrous sulfate Synonyms: Ferriclear
'7H20 Copperas
Sugar sulfate
Green vitriol
Alternate chemicals: None
Common packages sizes: 50 and 100 Ib bags
Approximate costs: $2.85-3.85/100 Ib.
Purities (from manufacturer): 20% Fe (granular), 63-66#/ft'
and bulk density:
Bench test concentrations: 100 mg/ml (50-200 mg/ml)
Feed concentrations: 2^0 mg/ml (2 Ib/gal.)
End point determinations: Add to floe or dosage
Personal safety: Hazardous if inhaled or ingested. A mild irritant to skin
and eyes. Remove contaminated clothing and shoes - Flush with plenty of
water, ff swallowed and victim is conscious, have victim drink water or milk
and have victim induce vomiting. If swallowed and victim is unconscious or
having convulsions, call for help and to nothing except keep victim warm.
Special mixing methods: Mix for at least 5 minutes. Granules dissolve best.
Cautions: Solution formed is quite acidic.
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic
Pumps 5 Stainless steel 3'6
Fittings: Rubber/lead/ceramlc/Duriron
kg
Figure 82. Data sheet on Ferrous sulfate.
-------
Chemical name: Hydrochloric acid Synonyms: Muriatic acid
HC1
Alternate chemicals: Sulfuric acid (sometimes).
Common package sizes: 65, I45, 700 Ib drums.
Approximate costs: $6.85"$9.00/100 Ib.
Purities (from manufacturer): 22° Baume".
Bench test concentrations: 100 mg/ml HC1
Feed concentrations: 36% max-use of 18% dilute HC1 is safer.
End point determinations: pH
Personal safety: Vapor and liquid irritating to eyes, nose and throat.
Will cause difficult breathing. Move victim to fresh air. Liquid will
burn eyes and skin. Remove clothing and shoes. Flush affected areas with
plenty of water. If swallowed and victim is conscious, have victim drink
water. 00 NOT induce vomiting.
Special mixing methods: Evolves heat and fumes when mixed with water -
add acid to water in all situations.
Cautions: Beware of fumes from the system, wear goggles, rubber gloves, apron,
Severely burns skin. Always add acid to water to avoid danger of explosion.
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic
Pumps & Plastic/rubber/porcelain
Fittings:
lb.454 = kg
Figure 83. Data sheet on Hydrochloric acid.
412
-------
Chemical name: Polyelectrolytes Synonyms: Polymers
Alternate chemicals: Fed- or A12SO^.I8 H20
Common package sizes: 50 Ib bags or 55 gal. drums
Approximate costs: $2.00/# (need only small amounts so should purchase in
pound lots).
Purities (from manufacturer) 99* *»0-50#/ft
and bulk density:
Bench test concentrations: I mg/ml (0.5-1 mg/ml)
Feed concentrations: 0.5~l%
End point determinations: Floe formation
Personal safety: Do not breathe fumes or touch powder. Flush with plenty
of water.
Special mixing methods: Difficult to mix/add to rapidly swirling water/
mix at least I hour prior to use/mix and use the same day-
Cautions: Viscous fluids requiring mixing and high pumping rates.
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic/other
Pumps & Do not use aluminum or galvanized equipment.
Fittings: Use: plastic/stainless steel/cast Iron
kg
gal.x3.785 - 1
Figure 84. Data sheet on Polyelectrolytes,
-------
Chemical name: Potassium Permanganate Synonyms:
KMnO,
Alternate chemicals: None
Common package sizes: 50, 100, 150 Ib drums
Approximate costs: $52-69/100 Ib
Purities (from manufacturer): 97% minimum
Bench test concentrations: 10-100 mg/ml as KMnO.
Feed concentrations: 10%
End point determinations: Oxygen demand
Personal safety: Highly toxic if inhaled or ingested. High concentra-
tions are cuastic. A strong irritant. Remove clothing and shoes and
flush with water. If swallowed and victim is conscious have victim
drink water or milk and have victim induce vomiting. If swallowed and
victim is unconscious or having convulsions, call for help and keep
victim warm.
Special mixing methods: Will dissolve better in cold water: (an
oxidizing agent).
Cautions: Easily reduced by natural reducers (e.g., organIcs, sulfite,
nitrite, etc).
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic (low cone.)
Pumps S Cast iron, plastic/stainless steel/steel
Fittings:
= kg ^
Figure 85. Data sheet on Potassium Permanganate.
-------
Chemical name: Sodium Bicarbonate Synonyms: Baking soda
NaHCO,
Alternate chemicals: Sodium carbonate
Common package sizes: 100 Ib bags
Approximate costs: $6.95/100 Ib
Purities (from manufacturer) 99.6% 59-62#/ft 3
and bulk density:
Bench test concentrations: 100 mg/ml as MaHCO..
Feed concentrations: 60 mg/ml (0.5 Ib/gal.)
End point determinations: pH
Personal safety: Do not ingest or inhale. In case of contact with eyes
or skin, flush with plenty of water.
Special mixing methods: None - dissolves quite easily.
Cautions: Slightly alkaline - \% solution - pH 8.2 alkalinity increases
at higher temperatures.
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic/other
Pumps & Iron, steel, rubber, stainless steel
Fittings:
kg
ft3x.028 = m
Figure 86. Data sheet on Sodium bicarbonate
-------
Chemical name: Sodium bisulfite Synonyms:
NaHSCL
Alternate chemicals: Sodium metabisulfite or Sodium sulfite
Common package sizes: 100 Ib bags
Approximate costs: $18.05/100 Ib.
Purities (from manufacturer): 99% as Na2$205 70-80 #/ft 3 65.5£ S02
and bulk density:
Bench test concentrations: 50 mg/ml as NaHSO-
Feed concentrations: 60 mg/ml
End point determinations: Large ORP change.
Personal safety: Slowly release toxic gas if exposed to fire, water or acids
to produce a highly corrosive hazard. Prevent inhalation and ingestion of
solid and liquid. If inhaled move victim to fresh air, Irritating to eyes
nose, and throat. In case of contact, remove clothes and shoes and flush
with plenty of water. If swallowed, drink water or milk.
Special mixing methods: None
Cautions: Acidic solution - NaHSO,/eventually oxidized to sulfate.
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic/other
Pumps S Lead, rubber, glass, ceramic, chrome, nickel, stainless
Fittings: steel.
kg
ft3x.028 = m
Figure 87. Data sheet on Sodium bisulfite,
-------
Chemical name: Sodium carbonate Synonyms: Soda ash
(soda ash) Na2CO, Soda ash - 58%
Sol . soda
Alternate chemicals: Sodium bicarbonate
Common package sizes: 100 Ib bags
Approximate costs: $3.70/100 Ib
Purities (from manufacturer) 99% Na2CO-, 30-65#/ft3
and bulk density: 58% Na20 {sodium oxide)
Bench test concentrations: 100 mg/ml as Na2CO_
Feed concentrations: 120 mg/ml
End point determinations: pH
Personal safety: Avoid inhaling or ingesting. Move victim to fresh air.
Very caustic, will cause burns to skin and eyes. Remove clothing and
shoes. Flush affected area with plenty of water.
Special mixing methods: Mix at least 10-20 min/#/ga1. of added Na2CO,/
mixes with large evolution of heat.
Cautions: Alkaline solution (ph 11.6) hygroscopic solid.
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic/other
Pumps & Iron, steel, rubber hose
Fittings:
- kg
ft3x.028 » m3
Figure 88. Data sheet on Sodium carbonate.
417
-------
Chemical name: Sodium Hydroxide Synonyms: Caustic soda
(caustic) NaOH Caustic soda lye
Alternate chemicals: Potassium hydroxide
Ammonium hydroxfd-e (undesirable)
Common package sizes: 650 Ib drum - 50% solution/400 # flake
Approximate costs: $IO.-I2/IOO# (liquid) $21.60-27.55 (flake)
100
Purities (from manufacturer) 50% liquid 76% flake and bulk density
and bulk density:
Bench test concentrations: 100 mg/ml.
Feed concentrations: 12-50%
End point determinations: pH
Personal safety: Very caustic. Do not handle with bare hands, do not
ingest or inhale dust. Move victim to fresh air. In case of contact remove
contaminated clothing and shoes and flush with plenty of water. If
swallowed and victim Is conscious, have victim drink water or milk. DO NOT
induce vomiting.
Special mixing methods: Di1iquescent, causes poison - be careful not to
add solid too fast, solution feed is absolutely necessary/large heat
evolution when mixed.
Cautions: Very dangerous to handle - alkaHne to pH 12.9 - at 1% solution/
wear goggles, rubber gloves, aprons (rapidly adsorbs water and C0£ from air.
Materials for handling:
Tanks: Process - any
Pumps £ Cast iron, rubber, steel
Fittings:
lbx.454 = kg
Figure 89. Data sheet on Sodium hydroxide.
418
-------
Chemical name: Sodium Hypochlorite Synonyms: Chlorox
NaCIO Liquid bleach
'avi1le water
Chlorine bleach
Alternate chemicals: Calcium hypochlorlte
Common package sizes: 5, 15, 50, 1,000, *f,500, gal. (12.5%)
Approximate costs: $0.36 - O.WlOO lb
Purities (from manufacturer): 12.5? (available chlorine) 13.1 % Na & Cl
Bench test concentrations: 0.5~5% chlorine
Feed concentrations: 5-0%
End point determinations: Chlorine residual
Personal safety: Vapor or liquid harmful or fatal if inhaled or ingested.
Can cause burns upon contact with eyes or skin. In case of contamination
remove shoes and clothing and flush with water. If swallowed and victim
is conscious, have victim drink water or milk and have victim induce vomit-
ing. If swallowed and victim is unconscious or having convulsions, call
for help and keep victim warm.
Special mixing methods: Is a very corrosive material.
Cautions: Avoid breathing vapors/do not mix with ammonia.
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic/other
Pumps & Rubber, plastics, glass, ceramics
Fittings:
kg
Figure 90. Data sheet on Sodium Hypochlorite.
-------
Chemical name: Sodium Sulfate Synonyms: Glaubers salt
Na2S04
Alternate chemicals: Potassium sulfate
Common package sizes: 100 Ib bags
Approximate costs: $6.50/100 Ib
Purities (from manufacturer): 99-5%
Bench test concentrations: 100 mg/ml
Feed concentrations: 10-20%
End point determinations: Sulfate test
Personal safety: Do not inhale or ingest. Can be irritating to eyes or
skin. Remove clothing and shoes and flush with water.
Special mixing methods: Neutral solution pH 6-7 when mixed.
Cautions:
Materials for handling:
Tanks: Process - any
Chemical - any
Pumps & Stainless steel, rubber, plastic, cast iron
Fittings:
lbx.454 = kg
Figure 91. Data sheet on Sodium sulfate.
420
-------
Chemical name: Sodium sulfide Synonyms:
Na2S or Na2$.9H20
(Sodium sulfide enneahydrate)
Alternate chemicals: Ammonium sulfide
Common package sizes: 100 Ib drum
Approximate costs: $26.50/100 Ib
Purities (from manufacturer): 60-62%
Bench test concentrations: 50
Feed concentrations: 10%
End point determinations: Zinc acetate paper/removal of metal ion.
Personal safety: Yields sulfur dioxide and hydrogen Sulfide which is
extremely flamable and toxic on contact with acids or fire. Irritant-
remove victims clothing and shoes and flush with water. If swallowed and
victim is conscious have victim drink water or milk. Dust irritating to
nose, eyes and throat. Move victim to fresh air.
Special mixing methods: Mix slowly checkingpH add Ca(OH)2 or NaOH if pH
drops below 7/however most solutions are alkaline: should be used
immediately.
Cautions: Caution to avoid evolution of toxic t^S which occurs at low pH
values. Do not expose solid to air without the use of a self contained
breathing apparatus.
Materials for handling:
Tanks: Process - any
Chemical - any
Pumps & Cast iron
Fittings:
kg
Figure 92. Data sheet on Sodium Sulfide.
-------
Chemical name: Sulfuric acid Synonyms: 0?1 of Vitriol
H9SO. Battery acid
4 Fertilizer acid
Alternate chemicals: Hydrochloric acid
Common package sizes: 5 gal. carboys/ 55, MO gal. drums
Approximate costs: $8.40 - l5-35/IOO#
Purities (from manufacturer): 66° Baume1
Bench test concentrations: 50 mg/ml - f^SO^ ( IN)
Feed concentrations: up to 36% to use diluted at 25%.
End point determinations: pH.
Personal safety: Vapors are irritating to eyes, nose and throat. Move
victim to fresh air. Compound will burn skin and eyes. Harmful or
fatal if swallowed. Remove contaminated clothing and shoes and flush with
plenty of water. If swallowed and victim is conscious, have victim drink
water or milk. DO NOT induce vomiting.
Special mixing methods: Acid to water - ONLY - has high affinity for
water - add very slowly to reduce heat evolution.
Cautions: Corrosive and hygroscopic/very acidic pH 1.2, need goggles,
rubber gloves, aprons/burns skin. Heat evolved upon mixing/always add
acid to water to avoid danger of explosion.
Materials for handling:
Tanks: Process - any
Chemical - concrete/plastic
Pumps S Cone, steel/iron
Fittings: Dilute/lead, porcelain, rubber, glass
lbx.454 - kg
Figure 93. Data sheet on Sulfuric acid.
422
-------
7.9 SUPPLIERS INFORMATION
7.9.1 General
This section includes Information regarding sources of supply for the
various media and chemicals needed. The amounts of materials needed
have been calculated as Indicated in other sections, but this amount
should be verified with the manufacturer. It is critical that all of
these materials be ordered immediately since the shipping time may ex-
ceed 2k hours. It may be necessary to make special arrangements to
allow shipment to the spill site immediately.
The phone numbers of suppliers are Included where possible. To obta[n
treatment chemicals, the OSC should check with local suppliers, then
complete the table in this subsection and provide phone numbers to
handle all situations. Possible local sources are also listed.
7.9.2 Filter Supplies
Media
Coarse gravel:
Fi Her sand:
Fi Iter Coal:
(crushed anthracite)
Source
Local sand and gravel
dealer
Local water treatment
plant
Sandblast supplier
(to get sandblast
sand)
Local water treatment
plant
Ye 1 low Pages Heading
Sand and Gravel
Sandblasting Equip-
ment and Supplies
2.
Suppliers:
Carbonite Filter Company
P. 0. Box 1
Delane, PA 18220
717/W7-3350
Palmer Filter Equipment Co.
P. 0. Box 50
Falrview, PA
-------
7.9 • 3 Ion Exchange Media
Ion Exchange Media must be ordered from the following suppliers and in
formation transferred to these dealers regarding the specific waste-
water to treat:
1. Bio- Red Laboratories
32nd and Griffin Ave.
Richmond, CA
2. Dow Chemical Co.
2030 Dow Center
Midland, Ml 48640
517/636-1000
3. E.I. du Pont Nemours and Co. - Plastics Division
1007 Market Street
Wilmington, DE 19898
302/77^-2421
4. lonac Chemical Co. - Division Sybron Corp.
P. 0. Box 66
Bi rmingham Road
Birmingham, NJ 08011
609/894-8211
5. Mallinckrodt Chemical Works
P. 0. Box 5439
St. Louis, MO 63160
314/231-8980
6. Rohm and Haas Co.
Independent Mall West
Philadelphia, PA 19105
215/592-3170
7. Union Carbide - Linde Division
270 Park Avenue
New York, NY 10017
212/351-2345
7. 9'^ Granular Activated Carbon
Method of
Manufacturer _ Order Points _ Shipping Points Shi pmen t
Calgon Corp. Calgon Adsorption Systems Cattettsburg, KY Bags, 60 Ib
Box 1346 Bulk Truck,
Pittsburgh, PA 15230 20-40,000 Ib
412/923-2345 Rail, 80,000 Ib
424
-------
Manufacturer
Order Points
7405 Page Ave.
St. Louis, MO 63133
31V683-3200
4800 W. 34th St.,
Suite B-8
Houston, TX 77018
713/682-1301
Shipping Points
Houston
(Bayport), TX
Seattle, WA
City of
Industry, CA
Petrolia, PA
Witco 277 Park Ave.
Chemical New York, NY 10017
Corp. 212/644-6435
Westvaco Eastern States
J.F- Henry Chemical Co.
East Rutherford, NJ
Westvaco
Carbon Sales Dept.
Covington, VA 24426
Herbert Chemical Co.
Cincinnati, OH
Western States
Van Waters & Rogers
San Francisco,
Los Angeles, Portland,
Ken t, Den ve r
ICI America, Chicago, IL 312/775-4900 Marshall, TX
Inc. Dallas, TX 214/330-9580
Atlas New York, NY 212/688-1430
Chemicals Div.San Francisco, CA 415/341-5891
Wilmington, DE 302/658-9311
Los Angeles, CA 213/872-0127
Same
Same
Same
Same
Method of
Shipment
Bags, 60 Ib
Bulk Truck,
20-40,000 Ib
Bags, 60 Ib
Bags, 60 Ib
Bags or bulk
Bags or bulk
Bags or bulk
425
-------
7'3.«_5. Treatment Chemicals
Local Sources -
Chemical Use
Acetic Acid
Aluminum Sulfate
(Alum)
Calcium Chloride
Neutralization
pH control
Precipitant/
Coagulant
Precipitant/
Coagulant
Calcium Hydroxide Neutralization/
(Slaked Lime) Precipitant
Calcium Oxide
(Lime)
Ferric Chloride
Ferrous Sulfate
Hydrochloric Acid
(Muriatic Acid)
Neutralization/
Precipitation
Precipitant/
Coagulant
Reducing Agent/
Precipitant/
Coagulant
Neutralization/
pH control
Polyelectrolytes Coagulant ion
Potassium
Permanganate
Sodium Bi-
carbonate
Sodium Bisulfate
Sodium Bisulfite
Sodium Carbonate
(Soda Ash)
Oxidizing Agent
Neutralization/
precipitation
Precipitant
Reducing Agent
Precipitation
Possible Local Source
Grocery Store/Vinegar Industry/
Industrial Supplier
Water Treatment Plant Industry/
Industrial Supplier
Industry/Industrial Supplier
Agricultural Supply/ Water and
Wastewater Treatment Plant/
Industry/Industrial Supplier
Agricultural Supply/Water and
Wastewater Treatment Plant/
Industry/Industrial Supplier
Wastewater Treatment Plant/
Industry/Industrial Supplier
Wastewater Treatment Plant/
Industry (pickle liquor)/
Industrial Supplier
Industry/Industrial Supplier
Sewage Treatment Plant/Water
Treatment Plant
Industry/Industrial Supplier
Grocery Store/as baking soda
Industry/Industrial Supplier
Industry/Industrial Supplier
Industry/Industrial Supplier
Water Treatment Plant/Industry/
Industrial Supplier
-------
Chemical
Use
Possible Local Source
Sodi urn Hydroxi de
(Caustic Soda)
Sodium Hypo-
chlorite
Sod!urn Sulfate
Sodium Sulfide
SuIfuric Acid
Neutralization/
Precipitant
Oxidizing Agent
Precipitant
Reducing Agent/
Precipitant
Neutral i zation/
pH control
Industry/Industrial Supplier
As Bleach/Grocery Store/
Industry/Industrial Supplier
Industry/Industrial Supplier
Industry/Industrial Supplier
Industry/Industrial Supplier
When chemicals are not readily available locally, they must be ordered
from a manufacturer. The OSC should prepare a list of chemical sources
which includes a 2k hour phone number, the location of the regional
warehouse, and the availability of chemicals. The following format is
presented to aid the OSC in collecting sufficient information. The
chart should be completed for each of the 19 treatment chemicals.
7.10 CALCULATION AIDES AND DEFINITIONS
The following tables are designed to clarify the information which is
presented in the preceding subsections. It also eliminates the re-
quirement for definitions throughout the text by placing them in one
general listing. The following three subjects are covered:
Unit Abbreviations
- Gives the meaning of the
abbreviation, the definition
and unit type
Conversion Factors
Glossary
Common English to Metric con-
version factors are given as
are interconversion between
various weights and measures
- Terms used in the text are
defined regarding the context
in which they are used in this
report
^27
-------
Supplier and Office 2k Hour Amount Immed. Time Needed to
Chemical Location Phone Phone Available Order Larger Amount
.c-
N3
OO
Figure 9^. Format for chemical suppliers information
-------
Unit Abbreviations
Definitions Dimensions
Type of Unit
cm
fpm
ft
ft2
gal
gpd
gpm
2
gpm/ft
HP
hr
in
in. Hg
i
Ib
m
min
mg
m)
m3
N
n
P
n
s
PO!
OP
sec
Sp.g
cen t i me te r
feet per minute
feet
square feet
gal Ions
gal Ions per day
ga) Ions per minute
gallons per minute per
square ft
process height
hour
inch
inches of mercury
liter
pounds
meter
minute
mi 1 1 i gram
(1 /1000th gram)
mi 1 1 i 1 i ter
(l/1000th of a liter)
cubic meters
normal i ty
number of process tanks
number of sludge tanks
position of the interface
process flow rate
second
spec! fie gravi ty
L
L/T
L
L2
L3
L3/T
L3/T
L3/T
L2
L
T
L
L
L3
W
L
T
W
L3
L3
-
-
L
L3/T
T
-
length
velocity
length/time
length
generally surface area
vo 1 ume
volume/time
volume/time
loading rate
length
time
length
pressure
vo 1 ume
weight
length
time
weight
vol ume
vo 1 ume
concentration
-
length
vol ume/t ime
time
-
-------
Symbol
td
Defini ti
de ten t i on t i me
reaction
ons Dimensions
for T
ds time to desludge T
t ,
draw
'fill
*T
Vp
Vp (eff)
#
Q
%
time to draw
time to fill
total detention
process volume
T
T
time T
L'
corrected process volume L
pounds
pump
percent
W
-
-
Type of Unit^
time
time
time
time
time
vo 1 ume
vo 1 ume
weight
-
-
|"|f| chemical feed system
Engl ish
acre
acre-ft
Btu
Btu/lb
bu
bu
cfm
cfs
cfs/acre
Unit
1
cfs/sq mi Ie
cu ft
cu ft
cu in.
cu yd
cu yd/mi
cu yd/sq
°F
fathom
ft
ft-c
Ie
mi Ie
Conversion Factors
Mul tipl ier
0.405
1,233.5
0.252
0.555
35.24
0.03524
0.028
1.7
4.2
0.657
0.028
28.32
16.39
0.75
0.475
0.29
0.555 (°F-32)
1.8
0.3048
10.764
Metric Unit
ha
cu m
kg-cal
kg-cal/kg
1
cu m
cu m/min
cu m/min
cu m/min/ha
cu m/min/sq km
cu m
1
cu cm
cu m
cu m/km
cu m/sq km
°C
m
m
lumen/sq m
430
-------
gal
gal
gpd/acre
gpd/cu yd
gpd/ft
gpd/sq ft
gpm
gpm/sq ft
hp
in.
Ib
Ib/day/acre
Ib/day/acre-ft
1b/1,000 cu ft
Ib/acre/day
Ib/day/cu ft
Ib/day/cu yd
Ib/day/sq ft
Ib/ft
Ib/mi1 gal
mgd
mgd/acre
mi le
ppb
pcf
psf
psi
sq ft
sq ft/cu ft
sq in.
sq miles
tons (short)
tons (short)
4
3
9
0.003785
3.785
0.00935
5.0
0.0124
0.0408
0.0631
40.7
0.7457
2.54
0.454
11.2
3.68
16.0
0.112
16
0.6
,880
1.51
0.12
,785
,360
1.61
10~3
16.02
4.88
0.0703
0.0929
3.29
6.452
2.590
907
0.907
Taken From: The Journal of the Water
Pollution Control Federation
cu m
1
cu m/day/ha
1/day/cu m
cu m/day/m
cu m/day/sq m
I/sec
1/min/sq m
kw
cm
kg
kg/day/ha
g/day/cu m
g/cu m
g/day/sq m
kg/day/cu m
kg/day/cu m
g/day/sq m
kg/m
g/cu m
cu m/day
cu m/day/ha
km
mg/1
kg/cu m
kg/sq m
kg/sq cm
sq m
sq m/cu m
sq cm
sq km
kg
metric tons
1 m - 100 cm = 3-281 ft
Inches
36
12
1
39.37 in,
Centimeters
30.48
2.540
431
-------
Area
Square
Miles
1
—
--
__
Cubic
Feet
1
--
--
--
--
1 Imperi
1 cu ft
1 cu m -
Acres
640
1
__
--
1
1 mpe rial
Gal Ions
6.23
1
--
—
—
1 cu m =
al (UK) gal weighs
of water weighs 62
103 1 and weighs
Mi les per Feet per
Hour
1
__
--
Days
1
--
--
Tons
1
™ «•
™* ~
Second
1.467
1
--
Hours
2k
\
--
Pounds
2000
1
--
Square
Feet
« *»
A3.560
1
--
sq m = 10.76
Volume
U. S.
Gal Ions
7.481
1.2
1
--
--
35.31 cu ft
10 Ib 1
.43 Ib 1
1000 kg
Ve 1 oc i ty
Inches per
Minute
1056
720
1
Time
Weight
Grams
—
454
1
Square
Inches
w «•
—
144
1
sq ft
Cubic
Inches
1728
277.4
231
57.75
61.02
- 264.2 gal
US gal weighs 8.34
cu m weighs 2283 Ib
Centimeters
per Second
— —
30.48
0.423
Minutes
1440
60
1
Grains
— m*
7000
15.43
Square
Centimeters
— —
--
929.0
6.452
Liters
28.32
4.536
3.785
0.946
1
Ib
Ki lometers
per Hour
1.609
—
--
Seconds
86,400
3,600
60
Metric Tons
0.9078
-_
--
1 long ton = 2240 Ib
ppm = 1 mg/1 =• 8.34 Ib per mg
432
-------
Cubic Feet per
Second
1
1.547
Pounds per
Sq ua re I n ch
1
0.4335
0.4912
Discharge
Million Gallons
Dally
0.6463
1
1 in. per hour per acre » 1.008 cfs
1 cu m/sec = 22.83 mgd = 35.32 cfs
Pressure
Feet of Water
2.307
1
1.133
Gal Ions per
Minute
448.8
694.4
Inches of Mercury
2.036
0.8825
1
1 atm = 14.70 psia = 29.92 in. Hg «= 33-93 ft water = 76.0 cm Hg
Power
Ki lowatts
1
0.7457
Kilowatt-Hours
1
0.7457
Horsepower
1.341
1
Foot-Pounds
per Second
737.6
550
Work, En er gy, and Heat
Horsepower- British Thermal
Hours
Units
1.341
3412
2544
Kilogram-
Meters per
Second
102.0
76.04
Calories
8.6 x 105
6.4 x 105
Temperature
0
32
5
41
Degree Fahrenheit = 32 + |- x degrees Centigrade
10 15 20 25 30 35 40 45 50 55 60 C
50 59 68 77 86 95 104 113 122 131 140 F
Taken From: Fair, Geyer and Okun
Water and Wastewater Engineering (15)
433
-------
GLOSSARY OF TERMS
Accessibility - The ease and safety of approaching a site.
Acidi c - A solution which has acid properties and contains excess (over
neutral) concentration of hydrogen ions.
Activated Carbon Adsorption - A process by which granular activated car-
bon selectively removes some organics and inorganics by physical
surface attraction.
Adsorpt i on Capac ity - An indicator of the amount of contaminant a cer-
tain type of carbon can remove.
Aeration - The oxidation of contaminants by forcing air through a
solution of wastewater.
Alkaline - A basic solution which contains large amounts of hydroxyl
ions.
An I on - A negatively charged ion. (Anionic - possessing a negative
charge)
Backwash - Forcing water at a high flow rate in tne opposite direction
of operational flow to remove particulates that blind the media.
Ballast - A heavy material placed in a container to enhance the
stability.
Batch - 1. The volume of fluid equal to the process capacity of a tank.
2. An operation which is not continuous whereby all operations
are done on one volume in the same tank.
Bench Testing - Small scale procedures to establish the treatment para-
meters for a specific wastewater.
Breakthrough * A condition which occurs when a media's capacity for
removing a contaminant is exhausted.
Cation - An electron having a positive charge. (Cationic -possessing
positive charges)
Chemical Injection - The process of adding a treatment chemical to the
wastewater. Specific points of addition and methods are needed.
Chlorination - The oxidation of contaminants by addition of chlorine
or other chlorine compounds.
434
-------
Clarification - The removal of turbidity and solids from a solution
through the sedimentation or flotation process.
Coagulation - A physical-chemical process which involves the reduc-
tion of surface charges and the formation of complex hydrous
oxides.
Des1udg jng - Operation of removing settled material (solids) from
the bottom of a sedimentation or precipitation reaction tank by
pumping into a separate holding tank.
DetentionTime - The length of time a volume of solution is contained
in the treatment process. Does not include filling and drawing
time in this context.
Piffuser - A mechanical device that allows bubbles of air to be in-
jected into a solution. Various types are available from a small
porous stone to a tube of steel covered with porous bags.
Downtime - The time during which process flow is stopped and backwash-
fngT desludging and maintenance operations are performed.
Effective Size - That size of media that 10% by weight is smaller than
and 90% by weight is larger than.
Endpo ?nt - The indication of the process completion. The type depends
on the test being used.
EqualI ization Tank - /\n extra process tank used to balance 5neonsistant
flows and "provide an even flow of wastewater to downstream processes,
FjJJ. Time/Draw Time - The amount of time needed to fill (draw) a
process ^ank. Equivalent to the process volume of the tank di-
vided by either the system or pump flow rate.
FiItrat ion - The removal of particulate matter by passing a waste
stream through a bed of graded media.
Filtration Rate -»The flow of water through a unit of filter surface
area fl/min/m or gpm/ft ].
Fines - The small particles which are present with mb'it coarse media
and can cause surface blinding.
Floe - The enlarged particles that are formed after chemical addition
and contact. Generally a physiochemical reaction creates a
desirable large and distinct floe.
Flocculat ion - This is the opportunity for particle contact to allow
increased size of the particles. It is done at a speed just
fast enough to keep the materials in suspension without breaking
up the floe.
-------
Flotation - A unit of operation to separate solid or liquid particles
from the liquid phase which have a specific gravity less than
water.
Freeboard - In a process tank the vertical distance from the fluid
level to the top of the tank.
In S i tu - Within the system/in this situation referring to treatment
wTthin the contaminated water body.
Inorganic Contaminants - Spilled compounds consisting of any element
except carbon.
Insoluble - Not capable of being dissolved, generally considered in
water.
Ion Exchange - A process in which ions held by electrostatic forces
to functional groups on the surface of a solid or exchanged for
ions of a different species in solution.
Limiting Factors - Those variables (or variable) which establish a
maximum process flow rate through the system.
Mixing - To agitate sufficiently to blend the contents of a tank with
the added materials.
Neutralization - The adjustment of pH to approach a value of 7'•
Non i on i c - Possessing an excess of neither positive or negative charges.
Off S t ream T rea tmen t - Treatment of a contaminant by removing the
wastewater and treating it in a location adjacent to the waterway.
0rganIc Contarn i nants - Spilled materials which are compounds of carbon.
ORP - (Oxidation Reduction Potential) - A measurement of the positive
and negative ion concentration. Measured by a platinum electrode
on a meter.
Oxidation - The chemical reaction which involves a loss of electrons
by the waste species being treated.
Para 1 lei Operat i on - A mode of operation in which a wastewater is
treated by splitting the flow into a group of simultaneous pro-
cess units.
pH Meter - An electric meter which measures the pH by the use of a
calomel electrode. It may require manual temperature compensation.
pH of a Solution - pH is the negative log of the hydrogen ion con-
centration (- log [H ]) and is a measure of the intensity of acid
or alkaline condition of a solution.
£H_Pj3£e_r_ - Dyed paper which gives a rough indication of the pH (e.g.
H+ ion concentration) of the solution.
-------
precipitation - Treatment process in which reagents are added to
form insoluble products with the specific pollutants.
Presettler - A process tank used to remove the bulk of solids or
sludges that settles rapidly from a water column. It is cont-
inuously desludged and used when solids volume is greater than
3% of the flow,as well as in other applications.
Pretreatment - Early removal of certain contaminants to reduce the
load on downstream treatment processes.
Process Effluent - The treated fluid exiting a process element.
Process Head Loss - The pressure necessary to overcome the resistance
to flow through the process media and media supports.
Process Height - The height to which the tank is filled and it is equal
to the total height of the tank minus the freeboard.
Process Influent - The fluid entering a process element.
Process Tanks - Fluid containers in which batch treatment processes
are accomplished; geometry and size of these tanks are dependent
on the specific operation.
Process Volume - The total volume of wastewater that must be handled
during a certain unit process.
Pump Rating - The volume, headloss and type of wastewater that a pump
can handle in a certain situation. Defined by the fluid flow (GPM)
and the Total Dynamic Head (ft); these are the two coordinates of
the pumping curve from which the pump efficiency and horsepower
may be read.
Reactant - A substance or chemical participating in a reaction,in this
situation considered the chemical being added to a solution of
wastewater.
Reduction - The chemical reaction which involves a gain of electrons
by the waste species being treated.
Regeneration - A process by which the concentrated solution of the
exchangeable ion is passed through the bed. The contaminant is
then collected in this solution.
Saturat ion - A state of solution at which time it is in equilibrium
with excess solute and no more solute can be placed in solution.
Scaleup - Scaleup is the translation of bench test values to large
scale process units.
Sedimentation - The removal of solid particles from a suspension by
gravi ty settling.
Ser i es Operation - A mode of operation in which a wastewater is
treated by passing the entire flow through successive process
operations.
437
-------
Settling Rate^ - The speed with which a discrete particle falls through
the solution expressed in units of distance over time.
Sludge - The concentrated solids after sedimentation.
Slurry - A mixture of sol ids and 1iquid (usually water).
Spec i f i c Grav i ty - The ratio of the mass of a solid or liquid to the
mass of an equal volume of distilled water at A°C or of a gas to
an equal volume of air or hydrogen under prescribed conditions of
temperature and pressure.
Storage Tanks - Fluid containers such as equalization tanks and back-
wash storage tanks which do not contain the process operations but
nevertheless are necessary to accomplish the treatment scheme.
Supernatant - The clarified layer of wastewater above the sludge
layer after solids removal.
Surface B1inding - The situation which occurs in a filter due to the
hydraulic gradation during backwash. The fine media is near the
top of the bed so very rapid lead loss occurs in the first inch of
bed depth.
Time to Desludge - The amount of time needed to desludge. It depends on
the solids pumping capacity and the volume of sludge to be removed.
Underetrain - A mechanical barrier used to separate the cleaned water
from the media and to distribute the filter and backwash flows
evenly over the filter area.
Uniformity Coefficient - The ratio of the size such that 60% by weight
is smaller than the effective size i.e., the 60%/10% size.
Viscosi ty - A measure of the amount of resistance to flow. The higher
the "viscosity" the more difficult it is to make the fluid flow.
Volume of Spill ~ The entire volume of area contaminated by a spill
which must be treated or otherwise handled.
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8.0 STANDARD OPERATING PROCEDURES DURING CLEANUP
8.1 SAMPLING PROCEDURES
The collection and subsequent analyses of samples is important in evaluat~
ing the progress of the spill cleanup. As stated in Chapter 3 of this
manual (Methodology for Spill Assessment), it is also important to collect
samples as soon as possible after the spill occurs for spill identification
and assessment and for later use as evidence. L kewise, it is important to
collect samples at the beginning of and during the cleanup operation to
document the progress of the cleanup. The general sampling methodology
described here may be applicable to all situations, although the EPA "Fiefd
Detection and Damage Assessment Manual" (5) should be used as a guideline
when samples are to be collected specifically for assessment or enforce-
ment purposes.
8^. I . I Method of Sampl ing
There are two methods of sample collection: automatic and manual. "Auto-
matic" refers to the use of an automatic sampler to collect samples while
"manual" refers to collection of samples by a person at the scene. Sam-
pling at the scene of a spill will usually be performed manually because
of the emergency and temporary nature of the situation. Also, the presence
of personnel on the scene may make it convenient and economical to take
manual samples. Guidance, on selection and use of automatic samplers can
be found in other publications (65-6?). The following discussion will
assume manual sample collection although the theory could also apply to the
use of an automatic sampler.
8^1.2 ^Type of Samples
There are two types of samples which can be collected for analysis:
I. Grab (discrete samples).
2. Composite samples.
Grab or discrete samples characterize the water quality at a particular in-
.stant in time. The purpose of a composite sample is to mix discrete samples
in such a way to represent the average characteristics over a period of
time. In addition to generating an average value, compositing is often done
to reduce the analytical load placed on the laboratory.
The choice of the type of sample should depend on the objective of the sam-
pling and the variability of the water. If the variability of the para-
meter of interest is low (that is, if the concentration of the parameter
of interest changes little over tine), then a grab sample may characterize
the quality adequately. On the other hand, if the variability is high, then
a composite should be formed from grab samples taken at short intervals,
or the grab samples themselves should be collected and analyzed. If
nothing is known about the variability of the water, then grab samples should
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be collected and analyzed initially to determine the variability of the
water. Judgment will have to be exercised in terms of the allowed varia-
bility. As a general rule, though it is wise to form a composite sample
for analysis unless directed otherwise.
8.1.3 Types of Composi te Samples
A composite sample is a sample formed by mixing discrete samples taken at
periodic points in time or consisting of a continuous portion of the flow.
There are four commonly used methods of forming composites;
I. Constant tine - constant volume: samples of equal volume are taken
at equal increments of time and composited to make an average sample,
2. Constant time - volume proportional to flow increment: samples
are taken at equal increments of time and are composited propor-
tional to the volume of flow since the last sample was taken.
3. Constant time - volume proportional to flow rate: samples are taken
at equal increments of time and are composited proportional to the
flow rate at the time each sample was taken.
A. Constant volume - time proportional to flow increment: samples of
equal volume are taken at equal increments of flow composited.
In the case of continuous sampling the time intervals in methods I and 3
would be zero.
In many cases where a constant-speed pump is used, the treatment rate will
be constant so that the volume - proportional methods are identical to the
constant time-constant volume method. In this case the constant time -
constant volume method should be used. Continuous sampling is best when
it is feasible. Where the treatment rate is variable, a flow-proportional
compositing method should be used. Methods 2, 3» and 4 all give similar
results and the method which is easiest to apply should be chosen. Methods
I, 2, and 3 are the easiest to use since the time interval is constant and
a timer can be set to remind personnel to collect a sample. If a totalizer
is provided on the flow measurement device, method 2 should be used. If
a totalizer is not available but the record can be obtained from a flow
chart, the volume treated since the last sample was taken can be estimated
from the flow curve.
8.1.3.1 Mechanics of Compositing - For the "constant time-constant volume"
method, the contents of all the bottles can be poured into one container,
mixed, and the desired volume of sample withdrawn, assuming all the bottles
contain an equal volume. Alternately, the contents of each discrete bottle
can be mixed and an equal volume, as calculated below, can be taken from
each bottle for the composite;
V . - V
d c
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V, = volume of each discrete sample to be used
V = composite volume desired
n = number of discrete samples
For the "constant time - volume proportional to flow Increments" method, the
volume of each discrete sample to be used for the composite can be cal-
culated as follows:
V, F F
d s .. s
Where
V. = volume of the discrete sample to be used
V = composite volume desired
F = flow volume since last sample
F = estimated total flow volume
For the "constant time - volume proportional to flow rate" method, the flow
rate should be noted at the time each of the discrete samples was collected.
Then the portion of each discrete sample to be used for the composite can
be calculated from the equation:
ax + bx + ex = V
Where:
a, b, c = flow rates when discrete samples were taken
x = volume of sample/unit of flow
V = composite volume desired
So that
ax = volume of discrete sample "a" to be used
bx = volume of discrete sample "b" to be used
ex = volume of discrete sample "c" to be used
3^J .3.2 TJSampJJjK)__a_JSajtch_ Process - A single qrab sample or a number of grab
samples composited will often adequately characterize the discharge of
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effluent from a batch process. However, if a single sample or a small num-
ber of samples are to be used it is imperative that the contents be thorough-
ly mixed prior to sampling or in the case where quiescent conditions must
be maintained, a number of samples at various locations throughout the
process container should be taken.
3.1 .4 Sampling Location and Parameters
As a general rule it is recommended that samples be taken from the influent
and effluent of each process during the entire time of operation. This
will not necessarily result in an overbearing number of samples since many
samples will serve as the effluent from one process and the influent to
another process. Also, samples taken at frequencies as low as a few minutes
apart can be composited so that only one sample will result for subsequent
analysis.
Although it is obvious that the most critical sample to be taken is the final
effluent sample, there are many significant reasons for sampling at other
locations. Sampling of the raw flow coming to the treatment process is
important since this will allow a determination of the mass of contaminant
being removed when the raw is compared to the final effluent. This can be-
come especially critical in cases where it is difficult to get a represen-
tative sample of the contaminated watercourse and the only operational way
of determining the progress of cleanup is to measure the mass removed and
compare this to the original mass spilled.
Taking samples between treatment processes serves many purposes also.
samples allow a determination of the efficiency (or lack of efficiency) of
a certain process and then a decision can be made as to whether further opera-
tion of this process is required. Also, where filtration, adsorption or
ion exchange is used, sampling before and after a process allows calcula-
tions of the mass of solids, organics, ions, etc., that have been removed
by the process and it can be estimated in advance when backwashing, regenera-
tion or replacement wi11 be required. This will prevent the situation of
having to stop all operations because a filter has clogged or a column has
broken through when these problems could have been remedied during a pre-
vious "down time". By analyzing samples for such parameters as suspended
solids, total organic carbon, turbiflity, etc., in addition to the hazardous
material of concern, it will be possible to maintain good process control.
Also, some of these analyses can serve as indicators of the hazardous
material requiring fewer analyses of the hazardous material itself, which
oftentimes involves complex, expensive and long analytical procedure.
8.1.5 Sample Containers
Samp'es must be taken into appropriate sample containers to reduce the
possibility of contamination or adsorption which will yield incorrect re-
sults. The container must be completely clean and equipped with a tightly
fittinn cap. Organic hazardous materials must be contained in a glass jar
or bottle to reduce adsorption to the container walls. Specifically, oils
and grease, pesticides, or even short chain organic compounds should be
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placed into glass containers. Other materials such as metallic salts, can
be stored in plastic containers with no adverse effect.
Sample containers should be provided from the nearest analytical labora-
tory to insure use of the proper type or, if necessary, the bottles can be
purchased from a local bottle supplier. If possible, use wide mouth con-
tainers with a lined cap except where interaction between the sample and
cap material must be modified. (Then use narrow necked containers).
If commercial sample bottles can not be obtained, wide mouth canning jars
can be used If an aluminum foil liner is provided. Where a plastic container
is applicable, distilled water can be purchased, the bottles emptied and the
containers used when no other bottles are available. However, the use of
these bottles is not recommended without specific instructions from the OSC.
To clean sample containers prior to reuse, the following procedure has been
found to be effective:
I. Wash containers and caps with a non-phosphate detergent and scrub
strongly with a brush.
2. Rinse with tap water, then distilled water.
3. Invert to drain dry.
k. If additional cleaning is needed, rinse with sulfuric acid, tap
water and distilled water.
In certain cases, sample bottles are further rinsed with chemicals to re-
move traces of materials left by previous samples. These procedures are
outlined as follows:
I. Acid Rinse: If metals are to be analyzed, rinse the container with
a solution of one part nitric acid to four parts water, then with
distilled water. If phosphorus is to be analyzed, rinse the con-
tainer with a solution of one part hydrochloric acid to one part
water followed by distilled water.
2. Solvent Rinse: If oil and grease or pesticides are to be analyzed,
rinse the sample container with hexane, then acetone, and dis-
tilled water. The container should have been previously cleaned
with acid solution. Treat the container caps sinilarly.
For long term monitoring, however, the analytical laboratory performing
the analyses should provide prepared bottles for sampling.
3. I .6 Sample Preservation_ and IjJent i f icat ion
The purpose of sample preservation is to maintain the constituents of in-
terest in the same concentration as when the sample was collected. Even
with preservation, the concentrations of the constituents may be a
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function of the time between sample collection and analysis. Therefore,
for any given preservation method a maximum holding time is also speci-
fied. Other factors related to preservation that may affect the inte-
grity of the sample include the type and material of the sample container,
sample identification, and the chain of custody for sampling handling.
For tlio preliminary or initial sampling, icing or refrigeration of the
samples should be adequate. While not effective for all parameters,
icing or refrigeration is recommended as a standard technique since it comes
closest to being a universal preservative and does not interfere with any
analyses. The use of ice cubes and an insulated chest is usually an
effective and convenient method for storage and transport of samples.
For a long term sampling program or for process monitoring samples, the la-
boratory performing the analyses should be consulted for specific instruc-
tions regarding preservation techniques and sample containers.
3.1.6.1 Samp 1e I den t i f i cat i on - Once the sample is taken, certain proce-
dures must be followed to allow the identification of the sample and to
record the chain of custody. It is important that these techniques be stan-
dardized and become a part of normal field procedure.
Each sample should be assigned a unique number to allow easy identification
in the field and the laboratory. It is important that the number include
relatively few digits so that it will not be abbreviated during successive
handling. It is recommended that each person who samples be assigned a roll
of peel-back labels. These labels would include the person's initials and
sequential numbering. As a sample is taken and sealed, a number will be
affixed to the bottle. The label would include sufficient space for added
information such as date, preservative added, etc. Then the specifics re-
garding the sampling location, type of sample, and other pertinent facts
would be recorded in the field notebook.
8.1.6.2 Chain of Custody - In cases of litigation, there must be proof of
the chain of possession that occurs from the time of sample collection to
final destruction. If a sample cannot be traced completely, the validity
of the analytical result may be doubtful. Therefore, it is important that
procedures for a written record of chain of custody be included as normal
field practice. A person has custody of a sample if one of the following
requirements is fulfilled:
I. It is in his actual physical possession.
2. It is in his view after being in his actual physical possession.
3. It was locked up by him after being in his physical possession.
A. It was kept in a secured area, restricted to authorized personnel
after being in his physical possession.
When the sample leaves his custody, then a record should be made indicating
that this has been done.
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The most important aspect of field procedures Is to keep an accurate note-
book. Once the sample Is taken and a sample identification lab£l affixed
to the container, all pertinent information should be recorded in the note-
book. The following information should be included:
I. Sample identification number.
2, Date and time of collection.
3- Location of sampling point In detail.
k. Method used to collect the sample.
5. Volume collected and type of container.
6. Preservation method.
7- Analyses to be performed on the sample.
The person performing the actual sampling should be certain to sign and date
the record and, if possible, include the signature of a witness in the
sampling party.
After the labeling and notation, the sample should either be placed in a
chest which will be sealed or a seal"should be placed on the container
cover. The seal should be of a material which will readily indicate any
tampering. Then the person performing the sampling should record in the
field notebook how the sample was transported to the lab and indicate if any
analysis request sheet was sent with the sample.
If the sample was shipped, all receipts or shipping identification numbers
should be kept in the field notebook along v/ith the address of the reci-
pient. The signature of the person receiving the sample should also appear
in the notebook. The time and location of the sample while it was in cus-
tody of the sampling personnel should also be recorded in the notebook.
Whether or not a rigorous chain of custody procedure will be required for all
treatment process samples will be a decision of the OSC and his legal ad-
visors. However, it is estimated that these procedures will at least be re-
quired for the raw samples which may supply required data in later litigation,
8.2 RECORDS
The importance of keeping written records cannot be emphasized too strongly.
As documentation of the events surrounding the spill and its cleanup, these
written records may have important legal implications particularly in cost
recovery or reimbursement. The records may also serve as a learning tool
in that the knowledge gained from the spill can be applied to future spill
situations. It is a good practice after the spill is cleaned, and the
emergency is over, to go back and assess the measures taken at the scene.
Evaluation of this sort is important in improving response techniques. A
record of the progress being made in the cleanup is also important in making
decisions at the scene of the spill.
445
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It is recommended that the OSC keep in a permanent bound book a log or
diary of the chronological events from the 'minute of notification of the
spill until the cleanup and his duties are completed. All events of any
significance should be recorded in the log with notation of the date and
time. The information should include records of flow, operation, main-
tenance, sampling, fuel used, problems encountered, telephone conservations,
meetings held, orders issued, weather observations, etc. The log should be
kept in a bound, sequentially numbered notebook. Entries should be made in
the log immediately and the date and time indicated. No pages should be
removed from the notebook. If a page is ruined, it should be marked "VOID".
Important observations involving judgment and sampling records should be
signed by the principal investigator and countersigned by a witness.
The important records that should be kept in the notebook can be listed as
fo11ows:
I. General events - for each day start/stop times for cleanup activities,
arrival or procurement of equipment, documentation for authoriza-
tion, weather observations.
2. Treatment - gallons treated by each process, hours of operation
of each process, maintenance needed and/or performed, fuel used,
equipment breakdowns, ultimate disposal.
3. Sampling - records of sampling, sample preservation methods, and
destination and analyses required of samples.
k. Personnel - a record of all personnel on site, their function, and
the actual times present should be recorded. This is especially
important for those personnel, whether from a government agency or
third party contractor, associated with the cleanup/treatment
operation itself. It is imperative that the OSC develop a rigid
communication network with the person in charge of the cleanup/
treatment operation so that the OSC knows at all times the status
of each operation and the personnel attending the respective opera-
tion.
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SECTION V
METHODOLOGIES FOR SPILL PREVENTION
IN-PLANT SPILL PREVENTION
Management Cons i de r a t i on s
The full utilization of proper plant design and effective control systems is
essential for an effective spill prevention program. All control systems
are of little value unless backed by management committed to utilizing these
systems to their fullest extent. It is generally recognized that assignment
of responsibility to the smallest supervisory unit practicable is an effec-
tive management approach to improve performance. In spill prevention this
unit would be the smallest group of facilities that are physically separable
from others in terms of measurable pollutional loadings.
Management considerations for the prevention of spills are multitudinous.
Spill prevention objectives, investigation of spills to avoid a repetition,
and promotion of open and frank communication channels should be some of the
prime management objectives. All of these objectives aid in the rapid iden-
tification of spill sources and the minimization of spills (68).
Spills may be caused by mechanical failure or personnel error, or more
rarely, by fire, explosion, power failures, or "acts of God". However,
since most spills are a result of mechanical failure and/or personnel error,
the following measures can go a long way in preventing or minimizing their
occurrence (69):
Sound basic design
Thorough training of operating, technical and maintenance personnel
Strict job responsibility
Sound process control and alarm and monitoring systems ;,
Proper maintenance of equipment and facilities
Maintenance should review existing operating and maintenance procedures and
develop vulnerabi1ity studies. From these studies critical portions of the
manufacturing process can be singled out and modified to decrease the pro-
bability of a hazardous spill. The spill prevention program of any plant
should include an action diagram or plan to be followed when a spill occurs.
In this plan, responsibilities should be definitely assigned (preferably by
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name) to establish the chain of command so that there is no confusion or
time wasted. A primary consideration should be to prevent the spill from
contaminating the environment outside the plant (surface or groundwater,
municipal sewers, soil, etc.).
Physical means of stopping spills from reaching areas outside the plant
should be provided. Examples would include: maintaining neutralizing
agents near bulk storage areas, maintaining personal protective safety
equipment In potential spill locations so that spills may be localized.
V/hen lighter than water chemicals are handled, adequate length of flotation
spi11-contaminant booms or absorbent booms should be available along with
the proper means to deploy them. An adequate supply of dispersants (that
have been approved by state authorities) should be stored at the plant for
treatment of spills (70).
Plant Drainage
Proper plant drainage is a prime means of containing hazardous material
spills and preventing them from reaching receiving waters. When a drain-
age system is designed, consideration to entrapping as much potentially
polluted water as possible and diversion of t-.hese waters to the proper final
destination are the predominant concerns (70.
The following recommendations relative to plant drainage were part of the
Guidelines for Spill Prevention, Containment and Countermeasure Plans
(SPCC) (72).
I. Drainage from diked storage areas should be valve-restrained to pre-
vent a spill or other excessive leakage of a product into the
drainage discharge or in-plant effluent treatment system.
2. Valves used for the drainage of diked areas should, as far as prac-
tical, be of manual, open-and-close design. The condition of the
retained stormwater should be determined before drainage, es-
pecially if such drainage of impounded waters goes into watercourses
and not into wastewater treatment plants.
3. All plant drainage systems, if possible, should flow into ponds,
lagoons, or catchment basins designed to reta-in materials less
dense than water. Consideration should also be given to possible
chemical reaction, if spilled chemicals are commingled.
4. If plant drainage is not engineered as above, the final discharge of
all in-plant drainage ditches should be equipped with a diversion
system that could, in the event of an uncontrolled spill, be returned
to the plant for treatment, the objective being to work toward a
closed-cycle system.
5. Where drainage waters are chemically treated in more than one treat-
ment unit, natural hydraulic flow should be used. If pump transfer
448
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is needed, two "life" pumps should be provided, and at least one of
the pumps should be permanently Installed.
Monitoring Process Variables
The monitoring of physical and chemical quantities involved in plant pro-
cesses is an extremely useful aid in avoiding hazardous spills. Either
specific apparatus or entire process systems are commonly monitored. Nor-
mally process variables such as temperature, pressure, flow, specific gravity.
viscosity, and chemical composition are measured. Often these measuring
devices are used with automatic controls which regulate process variables
to achieve optimum utilization of raw materials. In order to do this, the
control keeps process variables within predetermined specifications. Such
a device may also have a vital role during abnormal situations triggering
corrective action, or, in extreme cases, in safely shutting down the system.
When monitoring hazardous materials, it is normal to use redundant or back-
up instrumentation. Because the sampling probe is in direct contact with
the usually extreme condition of heat and corrosive vapors, it is the least
reliable part of the system. Frequently it is desirable to use a device
having a different principle of measurement as a backup unit. An example
of this is the use of a resistance bulb to sense the operating temperature
of a reaction vessel. The backup device could be a thermocuple.
After determining that something is wrong, the proper corrective action
should be initiated. The corrective action depends entirely on the nature
of the hazard and the consequences to the plant or operation. An electrical
interlock system to shut down pumps and close valves leading to the process
unit which is malfunctioning is a common device to prevent more material
from being added to a potential spill.
Monitoring equipment should warn personnel that an operating abnormality
has occurred. Commonly a flashing light and horn, which can be silenced by
the operator, are used to attract the operator's attention to a particular
control loop. Operation of the alarm should be independent of any control
mechanism so that the alarm will still function properly even though a
malfunction might occur in the control mechanism. Further monitoring
equipment, such as a siren, should be employed to signal hazardous situa-
tions that might require evacuation of personnel from the area. Monitor-
ing systems can also be obtained which use prerecorded messages to in-
dicate the nature of the problem for the operator (73).
Inventory control systems and materials balance determinations may also
indicate if leakage or spillage is occurring. The hazard potential of the
following should be determined (69).
Raw materials Waste materials
Intermediate process compounds End products
By-products
449
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In-PI ant Piping
Pipelines used for in-plant transportation of hazardous materials should be
constructed or modified so that the following SPCC guidelines are adhered
to (72).
I. Each product pipeline should be clearly marked by lettering (coded
or otherwise), color banding, or complete color coding to indi-
cate the product transferred therein. The coding should conform
with company policy or standard plant practice which, in turn,
should conform with state or federal requirements.
2. Each oil or hazardous material product-fill line which enters
a tank below the liquid level should have a one-way flow check
valve located as closely as possible to the bulk storage tank. In
addition to confining the product to the tank, in the event of
valve or pipeline failure, the check valve should permit overhaul
of the main shut-off valve and should aid in preventing shock
loading of the pipeline and valves from a "slug" of the tank con-
tent caused by backflow into an empty fill line. As far as practi-
cal, the product flow in suction lines should be controlled by
use of a positive displacement pump.
3- Buried pipelines should be avoided. However, buried installations
should have a protective wrapping and coating and should be
cathodically protected if soil conditions warrant. A section of the_
line should be exposed and inspected annually. This action should
be recycled until the entire line has been exposed and examined on
a regularly established frequency. An alternative would be the
more frequent use of exposable pipe corridors or galleries.
I*. When a pipeline is not in service, the terminal connection at
the transfer point should be capped or blank-flanged, and marked
as to origin.
5. Wood-to-metal should be avoided as a pipeline support since it is
apt to retain moisture and cause pipeline corrosion which, when
coupled with the abrasive action caused by the pulsating action
of the line, could cause line failure with resulting leakage.
Supports should be designed with only a minimum point of surface
contact that allows for the pulsating movement (expansion and
contraction) of the line (i.e., rollers).
6. All above-ground valves and pipelines should be subjected to a
regular monthly inspection at which time the general condition
of items, such as flange joints, valve glands and bodies, catch trays,
pipeline supports, locking of valves, and metal surfaces, should
be assessed.
7. Elevated pipelines should be subjected to constant review to
450
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insure that the height of vehicular traffic granted plant entry
does not exceed the lowermost height of the elevated line; gate
check-in and in-plant travel routes warrant attention in this
respect.
8. As far as practical, all pumps should be located as close as
possible to the storage tank.
9. Flapper-type drain valves should not be used to drain diked areas.
Such drain valves should be of manual open and close design, and
they should be kept in the closed position when not in service.
The drain lines from dike areas should drain directly or in-
directly into treatment or holding tanks or ponds or catchment
bas ins.
Solid Material Storage
Solid material storage should conform to the following SPCC guidelines (72):
I. The open stockpiling of ores, chemicals and minerals should be
discontinued. Piles of bulk material should be covered to prevent
leaching and runoff. If open shed-like structures are used for
bulk storage, retention curbing should be provided around the
perimeter of the pile, or perimeter drainage trenches should di-
rect runoff into a suitable wastev/ater treatment facility.
2. Bulk storage should not be positioned on the natural earth. Storage
pads of concrete or other impervious materials should be used as
a base to prevent ground water leaching and percolation into the
earth.
3- Metal and fiber containers should be loaded, stored, and unloaded
so as to minimize possibility of container damage. The containers
should be stored In a covered area, off the ground in a manner which
will preclude damage and weathering to the container, and subse-
quent leakage. The area itself should be provided for drainage to
a treatment facility in an analogous manner to diked storage tank
areas.
4. If some conainers contain corrosive substances, these should be
stored so that leakage of these substances will not corrode through
adjacent containers.
5. All items outlined under this heading should be periodically inspected
to insure physical and mechanical integrity of the drainage and
containment systems.
Bulk Storage
Bulk storage of materials should conform to the following SPCC guidelines (5):
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I. No tank should be used for the storage of oil or hazardous sub-
stances, unless its material and construction are compatible
with the material stored.
2. All bulk storage tank installations should be planned so that a
secondary means of containment is provided for the entire contents
of the largest single tank. Dikes, containment curbs and pits
are commonly employed for this purpose, but they may not always
be appropriate. An alternative system would consist of a complete
drainage trench enclosure arranged so that a spill could termi-
nate and be safely confined in an in-plant catchment basin or
holding pond.
3- Drainage of rainwater from the diked area into a storm drain or
an effluent discharge that empties into an open watercourse, lake,
or pond, and by-passing the in-plant treatment system may be
acceptable if:
I. The by-pass valve is normally locked closed.
2. Thorough analysis of the rainwater ensures compliance with
applicable water quality standards.
3. The by-pass valve is unlocked, and relocked following
drainage under the supervision of responsible manage-
ment .
J». Adequate records are kept of such events.
A. The storage tanks located immediately adjacent to the dike itself
should be oriented with respect to the dike so that no manholes
face the dike. This is considered desirable, so that if a manhole
fails, the resulting discharge from a full tank will not be aimed
over, or at the dike.
5. If storage tanks located immediately adjacent to the dike itse'lf
are equipped with fill lines which enter the tank near the bottom
and if the fluid pumped has suspended abrasive material, the dis-
charge into the tank should be on the dike side, discharging against
the tank side away from the dike. Alternatively, a baffle plate
located inside the tank opposite the pump discharge in the area
apt to be abraded, may be provided.
6. Buried storage tanks represent a potential for undetected spills.
A buried installation, when required, should be wrapped and coated
to retard corrosive action. In addition, the earth should be
subjected to electrolytic testing to determine if the tank should
be further shielded by a cathodic protection system. Such buried
tanks should at least be subjected to regular hydrostatic testing.
In lieu of the above, arrangements should be made to expose the
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outer shell of the tank for external examination at least every five
years. A means of conducting regular internal examinations of the
tank at five-year intervals should be provided (down-hole television,
etc.).
7- Partially buried tanks for the storage of oil or hazardous materials
should be avoided, unless the buried section of the shell is ade-
quately coated since partial burial in danp earth can cause rapid
corrosion of metallic surfaces, especially at the earth/air inter-
face.
0. Above-ground tanks, depending on design (floating roof, etc.) should
be subjected to integrity testing, either by hydrostatic testing,
visual inspection, or by a system of nondestructive shell thick-
ness testing. When the latter system of integrity testing is used,
comparison records of shell thickness reduction should be main-
tained.
9. The foundation and/or supports of all bulk storage tanks should be
subjected to at least annual examination by a person with the
technical competence to assess the condition of the foundation and/
or supports.
10. To control leakage through defective integral heating coils, the
following factors should be considered and applied:
a. The past life span of internal steam coils should be
determined, and a regular system of maintenance and replace-
ment that does not exceed the anticipated life span
should be established.
b. To reduce failure from corrosive action, prolong life,
and reduce replacement costs, the temperature and en-
vironment have to be carefully considered when selecting
heating coil materials.
c. The steam return or exhaust lines from integral heating
coils which discharge into an open watercourse should be
monitored for contamination, or passed through a settling
tank, or skimmer, etc.
d. The feasibility of installing an external heating system
should also be considered.
II. Each bulk storage tank should be externally examined at least
once a month. Each inspection should include an examination of
streams, rivets, nozzle connections, valves, and pipelines directly
connected to the tank.
12. Mew and old tank installations should, as far as practical, be fail-
453
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safe engineered or updated into a fail-safe engineered installati
Consideration should be given to providing the following devices;
on
a. High liquid level bell or horn alarms with an audio sig-
nal at a constantly manned operating or listening station;
in smaller plants and audible air vent may suffice.
b. Low liquid-level alarms with an audio signal at a constantly
manned operation of listening station; such alarms should
have a non-bypassing reset device that can be readjusted
to a given operating level following tank fill or liquid
removal .
c. High liquid-level pump cutoff devices set to stop flow at
a predetermined tank content level.
d. Direct audible o'" code signal communication between the
tank gauger and the pumping station.
e. At least one fast response system for determining the
liquid level of each bulk storage tank such as digital
computers, telepulse, or direct vision gauges.
13- "Normal" plant effluent should be constantly monitored by a proven
monitoring system, and any deviation from normal should be engineered
to activate a visible readout recorder with an audible alarm that
can be heard at a constantly manned operation or listening station.
If practical, the monitoring device should be designed to operate a
bypass to release the effluent discharge into a holding pond.
\k. Visible product leaks from tank seams and rivets should be promptly
corrected.
15. Tanks should not be used with the knowledge that the "head" or "top"
is in a corroded-through condition. Action should be taken to
drain such tanks and repair the defective member as promptly as
poss ible.
16. When practical, each bulk storage tank should be lettered (code or
otherwise) or color coded to indicate its chemical content, the
Manufactur ing Chemists Association or Department of Transportation
coding being preferred, and the coding should duplicate those used
for chemical transportation identification.
17- The use of wooden tanks should be confined to water storage and
should be avoided for liquid chemical storage.
The Manufacturing Chemists' Association has developed a checklist to aid in
developing spill prevention and control programs for chemical plants. This
checklist is presented in the end of this section.
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SPILL PREVENTION DURING TRANSPORT
General Con s i der a t i on s
The Code of Federal Regulations (CFR) , Title *»9, Parts 170-17" was originally
published by the Department of Transportation to control surface transpor-
tation of hazardous materials. For air transport, more specific controls
were deemed necessary and the Federal Aviation Regulations (FAR), Vol. VI,
Part 103 were drafted to modify 49 CFR. CAB 82 is an air line tariff which
must be followed where it is more restrictive than '49 CFR or FAR 103. The
International Air Transport Association (IARA) Restricted Articles Regu-
lations must also be followed for all U.S. import and export shipments.
Within the U.S., state and local agency requirements must also be met.
All the regulations are designed to prevent spills from occurring and to
protect life and property- In complying with the regulations, the following
activities are required.
I. Identification by proper DOT nane
2. Classification by DOT hazardous material class
3. Packaging
4. Marking and labeling
5. Preparation of shipping papers
Both shippers and carriers are legally obligated to comply with the applica-
ble regulations. Before a shipment is consigned to a carrier, the following
must be checked by the shipper
I. That DOT authorized containers have been used.
2. That proper closures have been used and no leaks are evident.
3. That outside packages are properly labeled and have required outside
marking.
k. That shipping documents include proper DOT shipping name, hazardous
material class, signed certificate, proper count and weight.
Abbreviations must not be used for required entries.
5. Tliat non-compatible materials are not tendered in the same shipment.
If non-cornpat ible shipments are tendered to the same carrier,
make certain that the carrier recognizes the situation. Check the
loading and storage charts.
6. That the driver is made aware that the shipment contains a hazardous
mater i al .
7. That a carrier representative has an opportunity to approve the
-------
placenent, securing and blocking of the material before closing out
and sealing the load (if seals are used), if the material is loaded
oy the shipper's personnel.
8. That placards are properly displayed before the carrier leaves.
The .carrier should check that the shipper has met his requirements before
accepting a shipment. In addition, the carrier's personnel have certain
responsibilities regarding spill prevention (75).
Freight
I. Must have broad hazardous material knowledge involving proper DOT
shipping names, classes, required packaging, compatibility, la-
beling, marking requirements, placarding and shipping documents.
2. Must check hazardous material freight against documents. If
they do not check out, make certain that the discrepancies are re-
solved before freight is allowed to move any further.
3. Must refuse to accept hazardous material freight from shippers or
interline carriers if the shipping documents are improperly prepared
or do not check out with the freight involved or if the containers
are leaking, damaged or otherwise Improper.
4. Must inspect all hazardous material freight for leakage or damage
each time it is handled.
5. When damaged containers are discovered, must isolate and make
certain they are not moved until they are in proper condition for
further transportation. Make certain that all container informa-
tion is obtained for use in preparing the required report to the
Department of Transportation. (NOTE - In some instances immediate
telephone notification to DOT is also required).
6. When contamination occurs or when it is necessary to dispose of
hazardous materials or containers, must make certain that a quali-
fied individual supervises such activities.
7- Must make certain that non-compatible hazardous materials are not
loaded into the same vehicle.
3. Must make certain that proper placards are placed on vehicles when
required and that placards are removed or covered when not required.
9. Must make certain that hazardous material containers will not be
damaged by other freight or by nails or rough sides and flooring
within the vehicle.
10. Must make certain that all hazardous material is properly blocked
456
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and secured before closing out vehicle.
II. Must make certain that class A or B poisons are not loaded with
foodstuffs or other contaminatlble cargo.
12. Must be familiar with, and have available for reference, provisions
of 49 CFR Part 177, Subpart B, titled "Loading and Unloading"
and Subpart C, titled "Loading and Storage Chart".
Drivers
I. Must have a broad hazardous material knowledge involving proper
DOT shipping names, classes, required packaging, compatibility,
labeling, marking requirements, placarding and shipping docu-
ments .
2. Must have in his possession, and available for immediate use, pro-
per shipping papers covering all hazardous materials loaded on
his vehicle.
3. Must have specific instructions (preferably written) as to handling
procedures in case of hazardous material incidents.
4. Must know what to do and what information to pass on to firemen,
police and others should emergency arise.
5. Must report all discrepancies and irregularities observed during
trip (including such things as leaking containers or defective
tank truck valves).
6. Must understand their responsibilities as to attendance require-
ments when transporting a hazardous material.
7. Must refuse to accept hazardous material freight from shippers
or interline carriers if the shipping documents are improperly
prepared or do not check out with the freight involved or if the
containers are leaking, damaged or otherwise improper.
For specific requirements shippers and carriers should check the appropriate
regulations. These regulations can be obtained as follows:
49 CFR Superintendent of Documents
U.S. General Printing Office
Washington, D.C. 20402
CAB 32 Airline Tariff Publishers, Inc.
Dallas International Airport
P.O. Box 17415
Washington, D.C. 20041
457
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IATA Restricted
Articles Regulations International Air Transport Assn.
ATTM: Mr. Gordon Young
1155 Mansfield Street
Montreal, Quebec II3PQ
In addition to these requirements it is recommended that emergency infor-
mation cards, describing actions to be taken in emergencies, accompany
the shipment. These Chemcards (Cargo Information Cards for Water Trans-
portation) were developed by and are available from the Manufacturing
Chemists' Association, 1325 Connecticut Avenue, M.W., Washington, D.C. 20009.
Rai
Equipment Features ~ The Association of American Railroads (AAR) favors
the use of relief valves on tank cars instead of rupture disks since a re-
lief valve will close once the pressure is reduced (76). The DOT Federal
Railroad Administration, Hazardous Materials Brancii recommends that valves
be placed internally or otherwise protected if they are to be placed on
the bottom of tank cars, as is becoming more common (76). Also recommended
are protective "skids" to minimize contact of the tank with exterior
forces in the event of an accident. The AAR has designed a coupler ("shelf
coupler") which is less likely to disengage due to vertical motion at the
time of derailment (76). If the couplers remain together, they are un-
likely to puncture a car.
Preventive Maintenance and Safety^ Precautions - Many spills can be prevented
and the severity of those which do occur decreased by the exercise of
maintenance checks and safety precautions (76).
I. Prevention of overloading - Pressure can be generated by thermal
expansion when a tank car is overloaded. This can cause failure
of a rupture disk or opening of a relief valve.
2. Routine Inspection - Tank cars should be routinely inspected for
dents, gouges, or other damage. The running gear should also be
checked. Gaskets should be routinely replaced, say, on an annual
basis. Caps and plugs should be routinely inspected and replaced
as necessary.
3. Closing of valves - The importance of tightly closing valves
should be emphasized to all employees.
'i. Placarding - The placarding regulations established by DOT should
be observed for all hazardous cargo.
5- Positioning of cars - The DOT regulations specifying the position-
ing of cars (3 ) containing hazardous substances should be followed
closely.
458
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The following guidelines have been provided by EPA for the development
of Spill Prevention, Containment and Countermeasure (SPCC) Plans by
industry (72).
Tank Car and Tank Truck Loading/Unloading
Relative to tank car and tank truck loading/unloading procedures, the re-
quirements and regulations of the Department of Transportation should be
met. The following recommendations should be emphasized.
I. A system of containment curbs should be used for tank truck un-
loading areas, using ramps to provide truck access into the con-
fines of the containment curb. The curb enclosure should be
designed to hold at least the maximum capacity of any single
tank truck loaded or unloaded in the plant.
2. A trenching system should encompass each railroad tank car un-
loading area. The trench should be designed to carry away
any spill to a catchment basin or holding pond, at least equal
in capacity to the capacity of the largest tank car loaded
or unloaded in the plant.
3. As a fail-safe precaution, an interlocked warning light or physi-
cal barrier system, or warning signs, should be provided in
loading/unloading areas to prevent vehicular departure before
complete disconnect of flexible or fixed transfer lines.
b. Prior to filling and departure of any tank truck, the lowermost
drain and all outlets of such vehicles should be closely examined
for leakage, and if necessary, tightened, adjusted, or replaced
to prevent liquid leakage while in transit.
Tr uckj ng
Egu ipment Fea t ure s - Anti-jackknife devices are effective but are expensive
and limit maneuverability. Bottom-loading and vapor-recovery units help
to prevent spills and air pollution (76).
Preventive Ma ? n tenancy and Sa fe _ty_P_reca_uJtj o_ns_- Routine inspection and
maintenence procedures should be performed as for railroad cars. In the
case of a truck, though, the driver may have greater personal responsi-
bility and he should inspect the rig before leaving for his destination
to make sure it is safe to operate. The driver should make sure he has the
shipping papers and that they contain sufficient information to identify
the cargo (chemical name, shipper, manufacturer, telephone numbers).
Placarding of the truck should be performed as required by DOT regulations.
The driver should consider the nature of his cargo in judging the appro-
priate driving speed. Also DOT regulations on drivers working hours per
week shouH he ^t-.rictly observed.
-------
SPCC Plan guidelines for tank truck loading/unloading were given in the
discussion on railroads.
Mari time
Equipment Features - Probably the construction feature that is most signi-
ficant in preventing maritime spills of bulk cargoes is the doublehull
vessel. For this type of vessel in many cases a collision or grounding
would affect only the outer shell and not the actual container of the
chemical cargo.
Preventive Maintenance and Safety Precautions - Routine inspection and
maintenance should be performed for vessels and loading/unloading fad 11-
These procedures are covered in the EPA SPCC Plan Guidelines (77) •
Barge Loading and Dock Site Facilities
SpilJ prevention, detection, containment, and safety practices here dictate
that:
I. All flexible hoses must be hydrostatical ly tested annually, and
inferior hoses must be discarded and replaced.
2. Barge loading lines must be routinely inspected during loading
operations.
3. Adequate mooring lines forward and after are secured to all barges
to minimize movement during loading.
k. Hoses must be water-flushed into the barges after loading.
Transporting Barges Through Territorial Seas
Transporting barges through territorial seas to the disposal sites must conr
ply with the U.S. Department of Transportation regulations. Special em-
phasis must be applied to insure that;
I. No permittee will knowingly send a barge to sea with leaks or
defects that can lead to a spill.
2. The tugboats employed for transporting the waste barges must be
inspected and must comply with U.S. Coast Guard regulations.
3. The ba'rge must carry the following permits and certificates;
a. An Environmental Protection Agency ocean dumping permit.
b. A U.S. Coast Guard consolidated certificate of enrollment
and license for coasting trade
1*60
-------
c. The International load line certificate issued by the
American Bureau of Shipping.
Drummed Wastes
I. Drums are stored on curbed concrete pad while the barge shipment is
being assembled. In the event a drum is damaged, any liquid
spilled must be soaked up and redrummed. Solids spills must also
be redrummed.
2. The barge is equipped with a toe board and railing to prevent
slippage.
3. The drums are stored on deck in two rows with a walkway in the
center. Each row of drums is secured firmly together with two
strips of 5 cm (2 in.) steel binding to prevent shifting of the
cargo.
l). If, in spite of the precautions taken to prevent emergecies and
accidents, a drum is dumped or lost in any manner and/or loca-
tion other than that specified, regardless of the circumstances,
the U.S. Coast Guard must be notified immediately and action will
be taken in accordance with their recommendations. A full re-
port of the incident and action taken must be filed with EPA
within 30 days.
Pi peline
Egui,oment Featu r es - Safety devices have been extensively relied upon
because of the extent of pipeline networks. These include fire detection
equipment with automatic alarm and shutdown, automatic extinguishing
systems, and closed-circuit television. Systems have been developed which
monitor the flow and pressure at points along the pipeline. If a varia-
tion in pressure is detected, the line can be shut down until the leak is
located and repaired (?8,79):
Preventive Maintenance and Safety Precautions - Routine inspection and
maintenance should be performed on the pipeline system. Aerial inspec-
tion is presently widely used to detect leaks or digging activity near the
pipeline (76). Markers indicating the presence of the pipeline should be
installed at all roads and other crossings where possible dredging or ditch-
ing might take place.
Ai rways
The best preventive measure for an air shipment is to be sure that the
hazardous material is properly packaged and identified as to the potential
hazard so that it will be properly handled by airline employees. This
will be achieved if the regulations on hazardous shipments are followed:
461
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For shipments within the U.S.
Federal Aviation Regulations, Vol. VI, Part 103
Code of Federal Regulations Transportation, Title 49, Parts 170-189.
CAB 82, Official Air Transport Restricted Article Tariff No. 6-D.
For international shipments all of the above plus;
International Air Transport Association Restricted Articles Regulations.
All applicable foreign law.
SAFETY OR PREVENTION DEVICES
Certain specialized devices can be employed by operating personnel as spill
prevention and control measures. These devices can basically be used, l)
to provide early warning or detection of a spill, and 2) to contain the
spill at an early stage.
Mon i tori ng/Detec t ion Dev i ces
In large industrial plants or industrial rivers the expense of installing
detectors may be justified. Union Carbide has successfully used continu-
ous total carbon analyzers, pH meters, and hydrocarbon vapor analyzers for
spill detection at its plants (80). Other devices have been found applica-
ble for detecting pollutants in water (81).
Device Detection of
Catalytic combustion sensor Volatile organics
Electrical conductivity sensor Ionic solutes
pH and specific ion probes Acids, bases, metallic pollutants
Multicolor transmissometer Less volatile organics
Colorimeter Heavy metals
It is simpler and often just as effective to monitor a process character-
istic rather than the hazardous chemical itself. Characteristics that
might be monitored include flow, temperature, tank level and pressure (6).
These devices can serve a warning function only or can be tied in to a
control device to automatically control, correct, shut down equipment, or
provide safe disposal of the overflow. For example, pumps could be shut
down and valves closed to prevent a spill from occurring or becoming worse.
Containnent/Contro1 Devices
The objective of these devices is to stop or contain the flow of the spill.
Excess flow valves are in-line safety devices that act to limit the flow
of liquids or gases out of a pressurized system. They will pass normal
462
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rates of flow; however, they will close against excess outward flow rates
in the event the pressurized system is opened to the atmosphere due to
pipe breakage or because of system misoperation. These devices are used
extensively in pressurized liquified gases and in chlorine tank car
discharge lines (73).
The automatic sealing imbiber valve is simply a metal cylinder with necked
openings at each end and filled, with imbiber beads retained by supported
porous membranes. Relying upon the void volume which naturally occurs in
a bed of packed spheres, the valve passes water freely. However, when con-
tacted by a hazardous fluid, the beads swell rapidly, stopping all flow
(82).
Other devices such as dikes, curbs, and container plugs are discussed in
other sections of this report. Examples of catchment systems that can be
used to prevent spilled materials from contaminating the environment are
shown on the following pages.
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MCA SPILL PREVENTION AND CONTROL
CHECKLIST FOR CHEMICAL PLANTS
«.! DEFINE ANI» ASSESS TIIE HAZARDS
OF MATEUIALS HANDLED
&U RawMater&tb
Haw ali raw nssterais been considered?
Haw the potential consequences of me of each
jaw siatcrial becsidsftEcd?
Has each raw •mtcrial been identified ia a spill
tatint guide?
Is the iaventorpseotrol of raw materials adequate?
3s the purchxgamor procurement section aware of
raw materials quality control effects on possible
hazards?
6.1.2 hut
»Compounds
Have all intermediates been identified?
What are the poggfele consequences of spillages
cC intermediate cdtqpsuads?
Have intermediates been considered in the spill
rating guide?
Do you have means for detecting and measuring
the losses of intermediate materials and compounds?
(5,1.3 End Pradacte
Have all end products been considered?
Have the potential consequences of spills of each
tad product been defined?
Has each end product been identified in a spDi
rating guide?
Is the inventory control of end products adequate?
6.1.4 Bj4*ro«!urfa and Waste Products
Have all by-products and waste products been
considered?
Have the potential consequences of spills of each
by-product and .waste products been denned?
Has cadi by-pepduct and waste product been
identified in a spill rating guide?
-Is the inventory control of by-products and waste
products adcauaftg?
6,33 Rati^Gekle
Has a ra&m fwfc beea prepared or considered?
Have Ihc frequency, detcctahiliiy, consequences,
And local conditions facjters hecn.considcrcd?
Have all raw materials, intermediates, by-products,
waste products, and end products been rated?
Wto bat access to and uses the rating guide?
63. ASSESS THE POTENTIAL OF SPILL
OCCURRENCE
&2.1 Receiving and Unloading
Has the "anything that can happen, will" phflot-
ophy been applied?
Arc the operations controlled and supervised by
dependable and knowledgeable personnel?
Are ioss«s monitored?
Are fnaintenance and preventive maintenance in-
spections reporting adequate?
6,2.2 Storage anil Transfer
Are all materials inventoried and controlled?
Is the best equipment utilized?
Are small spills reported and properly and
promptly handled?
Has the probability of a major spill incident been
established?
6.2.3 Process Operations
What is the .practice of controlling and reporting
emergency discharges?
Are process upsets and equipment failures repeti-
tive? If so, why? Are process errors recognized and
reported?
Do the operating personnel know and recognize
the detrimental effects of spills and accidental dis-
charges?
6.2.4 In-Process Transfer
What arc the practices of controlling and reporting
emergency discharges?
Arc process upsets and equipment failures repeti-
tive? If so, why?
Are process errors recognized and reported?
Do the operating personnel know and recognize
the detrimental effects of spills and accidental dis-
charges?
6.2.5 Lal»orotory and Pilot Operations
Are the potential ii! effects of accidental or unusual
discharges recognized?
-------
An spifl prevention and coatroh factors applied
ja planning and design?
Is there adequate
«f "
of the waste prod-
Itt
*H>osaia*dihaJ opera-
nd oodboifeaabd?
with spill prevention
to awbted and handled as a
personnel awan that the problem can't be
Joshed down the drain?
Ham personnel been alerted to the unusual haz-
ards involved in start-up and shutdown, especially
esaerfeacy shutdowns?
62.7 Mail
ric
Arc Muatcnance personnel aware of spill preven-
tion and control problems?
Do production, technical and waste control per-
sonnel coordinate with maintenance?
&2J Aniliary awl Support Operation*
Do these other departments recognize their in-
volvement in spill prevention and control?
Does overtaxing support equipment and opera-
•lions present spill problems?
63 EVALUATC INFLUENCING PHYSICAL
FAGKNB
6.3.1 Ms«sl51ii
Aft physical iKMn such as terrain and proximity
to reccmag water considerations hi planning. preven-
tion, and control of spitts?
Do the backup, stoppage, and overflow of waste
affect the overall programs for spills control?
Are dikes and other containment devices in-
fluenced by physical factors of slope, runoH. Rootling,
soil conditions, etc.?
h the property underlain by shaflm* |HH»nl waters
which would be subject to pollution via percolation
of spills through the soil?
633 Machinery anil Equipment
Are the existing plant machinery and equipment
significant factors in spill prevention?
Is related auxiliary and support equipment prop-
erly maintained?
Docs spill prevention and control equipment re-
ceive adequate inspection and preventive maintc-
e?
6.3.3 Buildings and Structures, Yard and
Ground*
What is the influence of buildings and other struc-
tures in the prevention and control of spills?
Are roof deposits potential spill hazards?
Are ground deposits potential spill hazards?
6,3.4 Operating Areas
Are spilled materials handled promptly and prop-
erly?
Do accumulations of small spills present a prob-
lem?
Can maintenance be performed without bypassing
safety devices and procedures?
utb-ly|>« spill mlchmcnt «ysten^
Depressed arc* form.
465
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etatnam to srooii
OS VATXKCCOBSK
CAPTURE VOLUME
K» FLOATABLE MATERIAL
ran
CONTROLUNO
niSCHAHUe RATE
^ r
Tocmr SEWKR
OH WUUSTHIAL
TREATMENT PLANT
CifcfeoMst bufa system of flow-tiuoofh tyjn,
Vtth ttriflre-mntrolUd dicciuiK* uto.
63.5 Sewerage System*
Arc sewers segregated or combined?
Cin spills be diverted to minimize effects?
b the plant sewerage system maintained properly?
Are blockages and back-up flooding a problem?
63.6 Storm Water Runoff and Collection
Has the effect of storm water been considered?
Caa storm water be diverted away from spill
Are roofs, buildings and ground a source of "Act
of God" spill effects?
Are storm water effluents measured, sampled and
rafaatcd?
63.1 Utilities and Utilities TmumiMion
Do spill prevention and control devices have ade-
quate uninterrupted power?
What is the effect of power interruption on alarms,
control systems, pumping, etc.?
Do the power plant and water treatment plant.
contribute to potential for spills?
6.3.8 Potential of Natural Disasters
Has the probability of natural disasters been deter-
mined or considered?
What areas could be affected by natural disasters?
Can waste treatment ponds be influenced?
Is sewerage back-up a problem?
STOKM srvr.it
* mocrss WASTKWATKR
ooo
~r"hoooo
T urn.i. mmm, nrwrn
O
o
Cute.
Midi,
CluMt
TMfc*
SssMjr?* i^l atchmcat lyttem.
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REFERENCES
1. U.S. Congress. Federal Water Pollution Control Act as amended. Public
law 92-500, 92nd Congress, S.2770. Washington D.C., Oct. 18, 1972. p. 89
2. Federal Highway Administration, Bureau of Motor Carrier Safety. Truck
Placarding Chart.
3. Code of Federal Regulations, Title ^9, Parts 170-179, Subchapter A
paragraph 17^-589. Hazardous Materials Regulations board.
k. Code of Federal Regulations. Title 1A, CFR, Part 103, Sec. 103.3.
5. U.S. EPA Field Detection and Damage Assessment Manual for Oil and
Hazardous Materials Spills. EPA Contract No. 68-01-0113. June 1972.
6. Department of Transportation and U.S. Coast Guard. Hazard Assessment
Handbook. CG * H6-3. Jan. 197**.
7. Marks, L.S. Mechanical Engineers Handbook, Fourth Ed. NY, McGraw-
Hill Book Co., NY, 19*41, p. 278.
8. Department of Transportation and U.S. Coast Guard. A Condensed Guide
to Chemical Hazards. Chris CG-M6-1 Jan.
9. Cargo Information Cards, (Chemcards), Manufacturing Chemists Association,
1825 Connecticut Ave, N.W., Washington D.C. 20009.
10. USEPA Oil and Hazardous Materials Technical Data Assistance System,
Division of Oil and Hazardous Materials, Office of Water Programs, EPA.
11. Perry, R.H. and Chilton, C.H., Chemical Engineers Handbook. McGraw Hill
Book Company. NY 1973. P. 7-32 - 7-33, 6-90 - 6-91.
12. Dawson, G.W., Shuckrow, A.J. and Swift, N.H. Control of Spillage of
Hazardous Polluting Substances. Federal Water Quality Administration
Report No. 15090 FOZ. November 1970.
IJ. Wilder, I. and Brugger, J.E., "Present and Future Technology Requirements
for the Containment of Hazardous Material Spills", Proc. of the 1972
National Conference on Control of Hazardous Materials Spills, p. 77-83.
\k. Pontius, P.W., "Containment and Disposal of Product from Leaking Drums
in Transit", Proc. of the 197** National Conference on Control of
Hazardous Material Spills, Aug. 197/<, p. 217-218.
-------
15. Friel, J.V., Hiltz, R.H. and Marshall, M.D., "Control of Hazardous
Chemical Spills by Physical Barriers", Environmental Protection Agency,
Edison, EPA-RZ-73-185, March 1973, p. 91.
16. Hiltz, R.H., "A Physical Barrier System for Control of Hazardous
Material Spills in Waterways", Proceedings of the 1972 National Con-
ference on Control of Hazardous Material Spills, March 1972, p. 85~92.
17- Johanson, E.E., Bowen, S.P.,."Recovery and Processing of Hazardous Spills
in Water", Proc. of the 197^ National Conference on Control of Hazardous
Material Spills, Aug. 1971*, p. 188-193.
18. Proposed EPA Regulations on Designation of Hazardous Substances, Section
311, P.L. 92-500, 40FR 59960 Dec. 30, 1975.
19. Ottinger, R.S., Blumenthal, J.L., Dal Portou, D.F., Gruber, G.I.,
Santy, M.J., and Shin, C.C., "Recommended Methods of Reduction
Neutralization, Recovery and Disposal of Hazardous Waste", Environmental
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A68
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28. Manufacturing Chemists Association Laboratory Disposal Manual,
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35. Personal communication to Rhodia Inc., Chipman Div., Portland, Oregon,
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Ohio, C. Shih, TRW, to G. Lawrence, 5/26/72.
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Treatment: Advanced Wastewater Techniques", Pollution Engineering,
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39. Kunz, R.G., Giannelli, J.F., and Stensel, H.D., "Vanadium Removal
from Industrial Wastewater", 30th Annual Purdue Industrial Waste
Conference, May 1975.
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from Tanker Oil Spills", WQO Environmental Protection Agency, 15080
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to Discharges of Hazardous Chemicals", U.S.C.G. NTIS-ADA-010-110.
469
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A3. Bauman, C.R. and J.L. Cleasby. Design of Filters for Advanced Waste-
water Treatment. Presented at Technology Transger Design Seminar.
Seattle, Washington. Oct. 31 and Nov. I, 1973, p. &•
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Reinhold Company, New York. 1971, p. 310
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Transfer. Oct. 1973, P 3-1 - 3-70.
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Process Applications. ICI American Inc. 197'•
48. Eckenfelder, W.W. and D.L. Ford. Water Pollution Control - Experimental
Procedures for Process Design. Pemberton Press, New Yourk. 1970, p. 269.
49. Rohm and Haas Company. Technical Bulletin Ion Exchange Department.
Amberlite IR 120 Plus and IRC Bk. Sept. 1969.
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International Textbook Company. Scranton, Pa. 1970, p. 27^-275.
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National Lime Association. Washington, D.C., 1968. p. 139.
52. Rushton, J.H. and J.Y. Oldshue. Mixing - Present Theory and Practice.
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1969, P. 351.
54. ASCE and WPCF, Sewage Treatment Plant Design, WPCF. 1959. p. 371.
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74. U.S. DOT Office of the Secretary, Operations Division, Office of Ha-
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472
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TECHNICAL REPORT DATA
(Please read Instructions on the reverse before completing)
1. REPORT NO.
EPA-600/2-77-22?
3. RECIPIENT'S ACCESSION-NO.
4. TITLE AND SUBTITLE
MANUAL FOR THE CONTROL OF HAZARDOUS MATERIAL SPILLS
Volume One - Spill Assessment and Water Treatment
Techniques
5. REPORT DATE
November 1977 issuing date
6. PERFORMING ORGANIZATION CODE
T.AUTHORIS) K> R< Huibregtse; R. C. Scholz; R. E.
WulIschleger; J. H. Moser; E. R. Bellinger;
C. A. Hansen
8. PERFORMING ORGANIZATION REPORT NO.
9. PERFORMING ORGANIZATION NAME AND ADDRESS
Envirex Inc., A Rexnord Company
Environmental Sciences Division
5103 W. Beloit Road
Milwaukee, Wisconsin 53214
10. PROGRAM ELEMENT NO.
1BB610
11. CONTRACT/GRANT NO.
Contract No. 68-03-2214
12. SPONSORING AGENCY NAME AND ADDRESS
Industrial Environmental Research Lab
Office of Research and Development
U.S. Environmental Protection Agency
Cincinnati, Ohio 45268
- Cin., OH
TVPF np REPORT AND PERIOD COVERED
Final -6/1/75 - 6/30/77
14. SPONSORING AGENCY CODE
EPA/600/12
15. SUPPLEMENTARY NOTES
16. ABSTRACT
A manual for control of hazardous material spills using improvised treatment systems
was developed under this contract. Spill control techniques have been emphasized,
although a brief overview of spill prevention methodology is Included. The main
body of the manual has been subdivided into eight chapters. The following topics
are covered: 1) notification, 2) an inventory of information sources, 3) identifi-
cation and assessment of human danger potentials, 4) determination of the best
handling method, including a thought guide question approach to specific spill
incidents and suggested treatment schemes for 303 hazardous chemicals, 5) safety
considerations and a limiting factor process design, 6) construction and operation
of five improvised treatment processes (filtration, carbon adsorption, ion exchange,
gravity separation and chemical reaction), 7) process components and treatment
chemicals and 8) standard sampling and record keeping procedures.
It is stressed that previous familiarization with the contents is necessary for
its effective use and that the improvised systems should be used only when other
equipment is unavailable. Suggested treatment schemes and procedures have not
been field tested, so extreme care must be taken to follow all safety precautions.
The report is submitted in fulfillment of contract 68-03-2214 by Envirex Inc. and
covers the period June, 1975 to June, 1977-
17.
KEY WORDS AND DOCUMENT ANALYSIS
DESCRIPTORS
b.lDENTIFIERS/OPEN ENDED TERMS
COSATI Field/Group
hazardous materials; water tanks;
contaminants; waste treatment; chemical
removal (water treatment); filtration,
ion exchanging, adsorption, clarification
Notification procedures,
chemical Identification
human danger assessment
information sources
treatability decision
13B
18. DISTRIBUTION STATEMENT
RELEASE TO PUBLIC
19. SECURITY CLASS (ThisReportj
unclassified
21. NO. OF PAGES
487
20. SECURITY CLASS (Thispage)
unclassified
22. PRICE
EPA Form 2220-1 (9-73)
473
U.S. GOVERNMENT PRINTING OFFICE: ] 978-757- 1W6622 Region No. 5~ I I
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