Federal Register / Vol. 58, No. 35 / Wednesday, February 24, 1993 / Proposed Rules 11201 

amended guidance.' The SIP call letters 

interpreted that guidance and indicated 

corrections necessary for specific, 

nonattainment areas. The nonattainment 

area encompassing Clark County 

Indiana is classified as moderate and is 

therefore, subject to the RACT fix-up 

requirement. Indiana's SIP revision 

request which it submitted in response 

to the SIP call letter, also responds to 

part of the RACT fix-up requirement. 

On April 10,1989, the IDEM 

submitted a new rule, 326 IAC 8-2-13, 

Marine Vessel Surface Coating. This 

new rule applies.to only one source, 

Jeffboat, located in Clark County Indiana 

which is designated nonattainment for 

ozone. Rule 326 IAC 8-2-13 was 

developed in response to the Act's 

requirement that all States adopt RACT 

for major VOC sources in counties 

unable to attain the ozone standard by 

December 31,1982, and which,were 

granted an extension of the ozone 

attainment dote until December 31, 

1987. The following provides a 

summary ofthe State's requirements.for 

marine vessel coating as contained in 

the submittal: 

1. Inorganic zinc preconstruction 

primer shall be applied using an 

automatic airless system with automatic 

electronic sensors designed to minimize 

overspray and (o limit primer thickness 

to no greater than 0.001 inches (0.0025 

millimeters) on plates and 0.00125' 

inches (0.0032 millimeters) on other 

structural elements; as determined by 

ASTM procedure D-1186-81 

(incorporated by reference in Indiana's 

rules), for all primer coating operations. 

2. As on alternative, the inorganic 

zinc preconstruction primer shall 

contain no VOC as delivered to 

applicator. If Jeffboat elects to apply 

such a coating, it shall notify the State 

thirty (30) days prior to tho chango. 

3. Jeffboat shall maintain doily 

records of the (a) tons and square feet of 

steel coated, and (b) gallons and VOC . 

content of preconstruction primer used 

in the automatic airloss systems. 

4. Jeffboat shall submit an annual 

. report containing the daily records 

required to tho State thirty (30) days 

after tho end of each calendar year.The 

annual report shall document tho 

method of application of oil 

preconstruction primer coatings and any 

operational changes which affect VOC . 

'Among other things, tho pro-amondmont 

guidance consists of tho VOC RACT portions of tho 

l*nsl-B7 policy, 52 FR 45044 (Nov. 24,1997); tho 

Hlunhook. "Issuos Relating to VOC Rngtilation 

Culpnints, Deficiencies find Deviations, 

Clarification to Appondix D of Novomber 24, 1907 

Firderol Rftgisler Notice" (of which nottco of . 

availability was publi.shod in tho Federal RnginlRr * 

on May 25, 191)0), and tho oxisting CTGs.. .'. ' 

emissions from tho automatic blast and 

priming lines. If an Inorganic zinc 

primer containing no VOC was not In 

use, the report shall document the 

current availability of such primers for 

the preconslruction priming operation 

at Jeffboat. 

III. USEPA's Analysis of the Proposed 

Rule 

IDEM asserts that it is not reasonable 

forjeffboat to use a waterborne zinc 

primer, as recommended in the 

"Development of Control Guideline 

Document for Selected Non-CTG 

Sources in Indiana".3 The State 

provided the following justification for 

this position: 

1. There are no waterborne primers 

available.to meet the requirement for a 

3-minute drying time necessary for 

Jeffboat to continue using the equipment 

currently at the plant. 

2. In order to uso a waterborne primer 

with a longer drying time, Jeffboat 

would have to make significant changes 

to its painting lines. 

3. Given Jeffboat's financial condition 

and tho current state ofthe market, the 

costs of conversion cannot be justified. 

However, Indiana has not adequately 

demonstrated that the requirements in 

Rule 325 IAC 8-2-13 represent RACT 

forjeffboat. Specifically, the USEPA 

maintains that: 

1. Jeffboat has not provided an 

adequate explanation of its basis for tho 

cost estimate for changes to the painting 

lines to accommodate the use of a 

waterborne primer. The cost analysis 

submitted by Jeffboat provided a list of 

equipment, capital, and operating costs 

for both new and relocated equipment, 

but the submittal did not include an 

explanation of why this equipment was 

needed or how the costs wore 

determined. 

2. Jeffboat has not provided a 

complete evaluation ofthe feasibility of 

add-on control equipment. For example, 

Jeffboat does not appear to have 

evaluated tho feasibility of controlling 

the omissions from only the spray 

booths or only the ovens through the 

use of add-on control devices. 

3. Even if Jeffboat can provide the 

documentation discussed above, thoro is 

no justification provided for specifying 

only a maximum allowable film 

thickness as RACT, and placing no 

constraint on tho amount of VOC per 

unit of applied coating. In addition, it 

should bo noted that the specified film 

thickness units are not internally 

* In ordor to assist Indiana in determining RACT 

for this source, the abovo-namod report was 

proparod by Engineering—Scionco for USEPA, 

Kogion V, and was provided to the State. 

consistent. A thickness of 0.001 inch is 

0.025 millimeters, not 0.0025 

millimeters as specified in the proposed 

rule. 

In addition to tho RACT deficiencies 

stated above, USEPA also notes that 326 

IAC 8-2-13(b) fails to define the phrase 

"minimize overspray," and fails to 

describe how the electronic sensors will 

be used to meet this requirement. The 

rule also needs to specify the test 

protocol which will be used to vorifv 

the allowable limits. 

IV. Summary of USEPA's Action; 

Request for Public Comment 

USEPA is proposing to disapprove 

this rule, Marine Vessel Surface Coating 

(326 IAC 8-2-13), because the State has 

not adequately demonstrated that the 

rule represents RACT for Joffboat. 

Therefore, the rule does not meet the 

requirement under section 182(o)(2)(A) 

of the amended Act that Indiana correct 

that rule so that it applies RACT as 

required by pre-amended section 172. 

Public comments are solicited on the 

requested SIP revision and on USEPA's 

proposed rulemaking action. Public 

comments received by April 26,1993, 

will be considered in tho development 

of USEPA's final rulemaking action. 

Under 5 U.S.C. 605(b), I certify that 

disapproving this rule will not have a 

significant economic impact on a 

substantial number of small entitios 

because it affects only one source, 

Joffboat. (See 46 FR 8709.) 

Under Executivo Ordor 12291, today's 

action is not "Major". It has been 

submitted to the Office of Management 

and Budget (OMB) for review. 

List of Subjects in 40 CFR Part 52 

Air pollution control, Environmental 

protection, Intergovernmental relations, 

Ozone. 

Authority: 42 U.S.C. 740l-7G71q. 

Dated: February 10,1993. 

David A. Ullrich, 

Acting Regional Administrator. 

|FR Doc. 93-4290 Filed 2-23-93; 8:45 ami 

BILLING CODE 6SW-S0-M 

40 CFR Part 63 

IAD-FRL-4560-3] 

National Emission Standards for 

Hazardous Air Pollutants for Source 

Categories: Organic Hazardous Air 

Pollutants From the Synthetic Organic 

Chemical Manufacturing Industry and 

Seven Other Processes 

AGENCY: Environmental Protection 

Agency (EPA). 
P.14 

lft02 Federal Register /Vol. 50, No. 35 / Wednesday, February 24, 1993 / Proposed Rules 

ACTION: Notice of public hearing and 

extension of public comment period. 

SUMMARY: On December 31,1992 (57 FR 

62608), EPA proposed standards to 

regulate the emissions of certain organic 

hazardous air pollutants from synthetic 

organic chemical manufacturing 

industry (SOCMI) production processes 

which are part of major sources under 

Section 112 of the Clean Air Act as 

amended in 1990 (the Act). This notice 

announces that EPA will hold a public 

hearing in Baton Rouge, Louisiana to 

hoar comments on the proposed rule. 

Tho public hearing will be held on 

March 18,1993. The period for 

receiving written public comments on 

the proposed rule is being extended. 

DATES: Comments. Comments must be 

received on or before April 19,1993. 

Public Hearing. The public hearing 

will bo held on March 18,1993 in Baton 

Rouge, Louisiana. The hearing will start 

at 6 p.m. and end at 10 p.m. 

Bequest to Speak at Hearing. Persons 

wishing to present oral testimony must 

contact EPA by March 12,1993. Each 

speaker will be allowed up to 10 

minutes, and each organization will bo 

allowed a maximum of 20 minutes. 

ADDRESSES: Comments. Comments 

should be submitted (in duplicate if 

possible) to the EPA's Air Docket (LE131), ATTN: Docket Number (see list 

following address) room M1500, U.S. 

Environmental Protection Agency, 401 

M Street, SW„ Washington, DC 20460. 

Comments that address areas pertinent 

to the proposed rule as a whole or that 

are applicable to more than one kind of 

emission point, such as general policy 

or legal comments, comments on the 

overall impacts ofthe standards, and 

comments on test methods should be 

marked ATTN: Docket Number A-90 -

19. Technical comments specific to 

process vents should be marked ATTN: 

Docket Number A-90-19; technical 

' comments about equipment leaks and 

any other comments about the 

negotiated regulation for equipment 

leaks should be marked ATTN: Docket 

Number A-90-20; technical comments 

about storage vessels should be marked 

ATTN: Docket Number A-90-21; 

technical comments about transfer 

operations should bo marked ATTN: 

Docket Number A-90-22; and ' 

comments specific to wastewater 

operations should be marked ATTN: 

Docket Numbor A-90-23. 

Public Hearing. The public hearing 

will be held at the Conservation Hearing 

Room at tho Louisiana Department of 

Natural Rosources. Persons interested in 

attonding tho hearing or wishing to 

present oral testimony should notify Ms. 

Kim Teal, Standards Development 

Branch, Emission Standards Division, 

U.S. Environmental Protection Agency, 

Office bf Air Quality Planning and 

Standards (MD-13), Research Triangle 

Park, North Carolina 27711, (919) 541 -

5580. 

Background Information Docket. The 

background information document (BID) 

for this rulemaking may be obtained 

from the U.S. EPA Library (MD-35), 

Research Triangle Park, North Carolina 

27711, (919) 541-2777. Refer to EPA453/D-92-016a, b, and c. The HON BID 

comprises throe volumos. Persons 

requesting copies of the BID should 

specify the volume(s) required, For 

information on the methodology and 

results of the analysis of national 

impacts, request BID Volume IA. For 

information on emission control 

technologies and cost procedures, 

request BID Volume IB. For information 

on the development of models for the . 

five kinds of emission points, request 

BID Volume IC. 

Dockets. The dockets listed above 

under ADDRESSES contain supporting 

information used in developing the 

proposed rule. Supporting information 

used in developing the negotiated 

standard for equipment leaks is 

available in Docket Number A-89-10. 

These dockets are available for public 

inspection and copying between 8:30 

, a.m. and 3:30 p.m., Monday through 

Friday, at the EPA's Air Docket Section, 

Waterside Mall, room M1500, U.S. 

Environmental Protection Agency, 401 

M Street, SW„ Washington, DC 20460. 

A reosonable fee may bo charged for 

copying. 

FOR FURTHER INFORMATION CONTACT: 

Dr. Janet S. Meyer, Standards 

Development Branch, Emission 

Standards Division (MD-13), U.S. 

. Environmental Protection Agency, 

Office of Air Quality Planning and 

Standards/Research Triangle Park, 

North Carolina 27711, telephone 

number (919) 541-5299. 

SUPPLEMENTARY INFORMATION: On 

December 31,1992 (57 FR 62608), EPA 

proposed standards to regulate the 

emissions of certain organic hazardous 

air pollutants from synthetic organic 

chemical manufacturing industry 

(SOCMI) production processes which 

are part of major sources under Section 

112 of the Clean Air Act as amended in 

1990 (the Act). The proposed notice 

announced that, if requested, a public 

hearing would be held in EPA offices 

located in Research Triangle Park (RTP), 

North Carolina. The EPA received 

several requests that the hearing be held 

in Baton Rouge, Louisiana to allow the 

affected community an opportunity to 

present oral testimony on the proposed 

rule. Tho March 18, 1993 hoaring in 

Baton Rouge was scheduled in response 

to those requests. The hearing scheduled 

for February 25,1993 will still be held 

at EPA offices in RTP because requests 

to speak at that hearing have already 

been received from several individuals. 

Dated: February 17,1993. 

Michael H. Shapiro, 

Acting Assistant Administrator, Office of Air 

and Radiation^ 

[FR Doc. 93-4291 Filed 2-23-93; 8:45 am] 

BILLING CODE 6SSO-CO-M 

40 CFR Part 86 

[FRL-4599-7] 

Control of Air Pollution From New 

Motor Vehicles and New Motor Vehicle 

Engines; Federal Test Procedure 

Review 

AGENCY: Environmental Protection 

Agency. 

ACTION: Notice of public workshop. 

SUMMARY: On March 9 and 10,1993, the 

Environmental Protection Agency (EPA) 

will hold a public workshop to inform 

interested parties of EPA's current and 

planned activities regarding the 

Agency's review of the Federal Test 

Procedure (FTP) for measurement of 

motor vehicle emissions. Section 206(h) 

of the Clean Air Act (CAA) requires EPA 

to "review and revise as necessary" the 

regulations governing the FTP to 

"insure that vehicles are tested under 

circumstances which reflect the actual 

current driving conditions under which, 

motor vehicles are used". 

DATES: The workshop will be convened 

at 8:30 a.m. on March 9,1993. Persons 

interested in making presentations at 

the workshop are requested to notify the 

Agency contact listed below at least two 

weeks prior to the workshop so that a 

final agenda may be prepared. Written 

comment may be submitted to the Air 

Docket (see ADDRESSES below) or the 

Agency contact until April 9,1993. 

ADDRESSES: The workshop will be held 

at the Sheraton Inn, 3200 Boardwalk 

Street, Ann Arbor, MI 48104. 

Telephone: (313) 996-0600. Materials 

relevant to the workshop are contained 

in Docket No. A-92-64. The docket is 

located at the Air Docket Room, room 

M-1500, Waterside Mall, 401 M Street, 

SW., Washington, DC, 20460. The 

docket may bo Inspected between the 

hours of 8:30 a.m. to 12 noon and from 

1:30 to 3:30 p.m. Monday through 

Friday. A reasonable fee may be charged 

by EPA for copying docket materials. 

FOR FURTHER INFORMATION CONTACT: John 

German, Certification Division, U.S. 
p.1 

OAR Box 1252 

Prepped by Candice Davis 

Document Number: 

38) FED REG VOL. 58, NO. 37 2/26/93 

Docket Number: 

A-90-22 

Printed 5/21/2008 3:16:06 PM Sheet 38 of 184 
P.2 

A-40-23-

Gosredtll©!^ Federal Sogistsr .. 

Vol. 58, No. 37 

Friday, February 28, 1993 

This section ot the FEDERAL REGISTERZZY.^ 

contains editorial corrections bJ prevkntsly 

published Presidential, Rule, Proposed Rule, 

and Notice documents. These corrections are 

prepared by fre Office oS fre Federal 

Register. Agency prepared corrections are 

issued as signed documents and appear In 

the appropriate document categories 

elsewhere in the issue. 

ENVIRONMENTAL PROTECTION •• •••' 

AGENCV-^ " ; 

40 CFR Part S3 

[AD-fRM53MJ ...'"-.•Z\...:-

National Emission Standards tor-; ;7 

Hazardous Air Pollutants to? Source 

Categories; Organic WaaanrdousAJr 

Pollutants front th® Synthetic Organic 

Chemical Manufacturing Industry and 

Seven ©their Processes ••.;':•/.••. 

Correction .. ''_-.., . ,• .".'..-. '.; YIn proposed rule document 92-28292 

beginning on page 62608 in the issue of . 

Thursday, December 31,1992, portions 

of §§63.128,63.131,63.143,63.144,... 

63.145, and 63.150 were illegible. For 

the convenience of the reader, the 

sections listed above are reprinted in.••'• 

their entirety.''

 r

~ 7^,r-r ::-.•;; y; 

'§63.128 -Trsnoter operations provision©— 

test methods' and procedures.'' -

(a) A performance test is required for 

determining compliance with the 

reduction of organic HAP emissions in 

§ 63.126(b) for all control devices other 

than: Vapor balancing systems; flares; 

and certain boilers and process heaters 

listed in paragraph (c) of this section. 

Performance test procedures are as • 

follows:, y 7 .- . . :-\y-' ... •.•.-.•: 

(1) A perfonnance test shall consist of 

three runs. 

(2) All testing equipment shall be 

prepared and installed as specified in 

the appropriate test methods. 7 

(3) For control devices capable of 

continuous vapor processing, each run 

shall represent at least one complete 

filling period, during whidi liquid 

organic HAP'a are loaded. r .... : y 

(4) Fo? intermittent vapor processing 

systems, eacTh ran shall represent at = , 

least one complete control defies cycla 

' - (5)Methbd.l£H'lA of part 60.-----V,.7:7....... 

appendix A, as appropriate, shall be . 

used for selection of sampling sites. 

(i) For an owner or operator 

complying with the 98-percen8 organic 

HAP reduction requirements in 

§ 63.126(b)(1), sampling sites shall be 

located as specified in paragraph 

(a)(5)(i)(A)or(a)(5)(i)(B). 

(A) Sampling sites shall be located at 

the inlet and outlet of the control 

device, except as provided in paragraph 

(a)(5)(i)(B). 

(B) If a vent stream is introduced with 

the combustion air or as a secondary 

fuel into a boiler or process heater with 

a design capacity lass than 44 

megawatts, selection pf the location of 

the inlet sampling sites shall ensure the 

measurement of total organic HAP or. 

TOC (minus methane and ethane), -

concentrations in all vent streams and 

primary and secondary fuels introduced 

into the boiler or process heater. A . 

sampling site shall also be located at the 

outlet of the boiler or process heater. 

(ii) For an owner or operator ;: 

complying with the 20 parts per million 

by volume limit in § 63.126(b)(1), the 

sampling site shall be located at the 

outlet of the control device. Y'-

(6) The volume exhausted shall be ..-.', 

determined using Method 2, 2A, 2C, or 

2D of part 60, appendix A, as 

appropriate. 

(7) For the purpose of determining 

compliance with the 20 parts per 

million by volume limit in 

§ 63.126(b)(1), Method 18 or Method 

25 A of part 60, appendix A shall be 

used to measure either organic 

compound concentration or organic 

HAP concentration, except as provided 

in paragraph (a)(9) of this section. 

(i) If Method 25A is used, the 

following procedures shall be used to 

calculate the concentration of organic 

compounds (Cr): 7 

(A) The principal organic HAP in the 

vent stream shall be used as the 

calibration gas. 

(B) The span value for Method 25A 

shall be twice the concentration being 

measured..•-...,. ,.-..-

(Q Use of Method 25 A is acceptable 

if the response from the high-level -

calibration gas is at least 20 times the 

standard deviation of the response from 

the zero calibration gas when the 

instrument is zeroed on the most 

sensitive scale. ...-•••; -j> •:. -,-i •.-.-.• 

(D) The concentration of TOC shall be 

corrected to 3 percent oxygen using the 

procedures and equation in paragraph 

(a)(7)(v) of this section. 

(ii) If Method 18 is used to measure 

the concentration of organic 

compounds, the organic compound : 

concentration (Cr) is the sum of the: 

individual components and shall be 

computed for each run using the 

following equation: 

• C T = L.C J 

where: 

Ct=Total concentration of organic 

compounds (minus methane and 

ethane); dry basis, parts per million 

by volume. :yy 

Q=Concentration of sample components 

"j", dry basis, parts per million by 

volume. '•' 

n=Number of components in the 

sample:-;•/ , 

. (iii) If an owner or operator uses 

Method 18 to compute total organic 

HAP concentration rather than organic 

compounds concentration, the equation 

in paragraph (a)(7)(H) of this section 

shall be used except that only organic 

HAP species shall be summed. The list 

of organic HAP's is provided in § 63.104 

of subpart F of this Part. 

(iv) The emission rate correction 

factor or excess air integrated sampling 

and analysis procedures of Method 3B 

of part 60, appendix A shall be used to 

detennine the oxygen concentration. 

The sampling site shall be the same as 

that of the organic HAP or organic 

compound samples, and the samples 

shall be taken during the same time that 

the organic HAP or organic compound 

samples are taken; 

(v) The organic compound 

concentration corrected to 3 percent 

oxygen (CJ shall be calculated using the 

following equation: 

C^=Gr 

17.9 

20.9 -ftO * 

where: 

Cc=C6ncentration of organic compounds 

corrected to 3 percent oxygen, dry 

basis, parts per milhon by volume. 

Cr=Total concentration of organic 

compounds, dry basis, parts per 

million by volume. 

%02d=Concentratlon of oxygen, dry 

basis, percent by volume. 

nam 
11668 - Federal Register / Vol. 58, No. 37./ Friday, Februaryv26, 1993:/ Corrections 

P.3 

(8) For the purpose of determining 

compliance with the 98-percent 

reduction requirement in § 63.126(b)(1), 

Method 18 or Method 25A of 40 CFR 

part 60, appendix A shall be used, . 

except as provided in paragraph (a)(9) of 

this section.

 ;r,> '-; 

(i) For the purpose of determining 

compliance with the reduction 

efficiency requirement, organic 

compound concentration may be 

measured in lieu of organic HAP 

concentration. 

(ii) If Method 25A is used to measure 

the concentration of organic compounds 

(Cr). the principal organic HAP in the 

vent stream shall be used as the 

calibration gas. 

(A) Ah emission testing interval shall 

consist of each 5-minute period during , 

the performance test. For each interval, 

a reading from each measurement shall 

be recorded. 

(B) The average organic compound 

concentration and the volume 

measurement shaii correspond to the 

same emissions testing interval. 

(C) The mass at the inlet and outlet of . 

the control device during each testing 

interval shall be calculated as follows: 

M^FKV.Cr 

where: 

Mj=Mass of organic compounds emitted 

' during testing interval), kilograms. 

V,=Volume of air-vapor mixture 

exhausted at standard conditions, 

20 °C and 760 millimeters mercury, 

standard cubic meters. 

Cr=Tofal concentrationof organic 

compounds (as measured) at the 

exhaust vent, parts per million by 

volume, dry basis. 

K=Density, (kilograms per standard 

cubic meter organic HAP). 

FsiO^^Cqnversion factor, (cubic 

•••••' meters orgamc HAP per cubic 

meters air) (parts per million by 

volume)-1. 

(D) The organic compound mass 

emission rates at the inlet and outlet of 

the control device shall be calculated as 

follows: 

Ei = -

E„ = -

n 

L M °J 

whiBre: 

Ei, Eo=Mass flow rate of organic 

compounds at the inlet (i) and 

outlet (o) ofthe combustion or 

recovery device, kilograms per 

hour." 

My, Moj=Mass of organic compounds at 

the inlet (i) or outlet (o) during 

testing interval j, kilograms. 

T=Total time of all testing intervals, 

hours. 

n=Number of testing intervals. 

(iii) If Method 18 is used to measure 

organic compounds, the mass rates of 

organic compounds (Ei, Eo) shall he.... 

computed using the. following 

equations:"' 

E,= ^(^CijMWijJQ i 

E0= K2 (LC()jMWo j\Qo 

\J= I •• . • : >••• • 

where: 

dj, (^Concentration of sample 

component "j" of the gas stream at 

the inlet and outlet of the control 

device, respectively, dry basis; parts 

per million by volume.

 ,; ;; -> 

MWy, MWoj=Molecular weight of 7 

sample component "j" of the gas 

stream at the inletand outlet of the 

control device, respectively, gram/ 

gram-mole. 

Oj,Qo=Flow rate of gas stream at the 

inlet and outlet ofthe control 

device, respectively, dry standard 

cubic meter per minute. 

K2=Constant, 2;494xl0~6 (parts per 

million).~' (gram-moleper 

standard cubic meter) (kilogram/ 

. gram) (minute/hour), where 

standard temperature for (grammole per standard cubic meter) is 

20 °C 

(iv) Where Method 18 or 25A is used 

to measure the percent reduction in 

organic compounds, the percent 

reduction across the control device shall 

be calculated as follows: 

E.-EQ 

* E, 

(100) 

where: 

R=Control efficiency of control device, 

percent. 

7 Ei=Mass emitted or mass flow rate "of 

organic compounds at the inlet to 

the combustion or recovery device 

as calculated under paragraph (a)(8) 

(ii)(D) or (a)(8)(iii) of this section, 

kilogram per hour. 

Eo=Mass emitted or mass flow rate of 

organic compounds at the outlet of 

the combustion or recovery device, 

as calculated.under paragraph 

(a)(8)(ii)(D);or (a)(8)(iii) of this 

section, kilogram per hour. 

(9) The owner or operator may use 

aiiy methods or data other than Method 

18 or Method 25A, if the method or data 

has been validated'according to Method 

301 of 40 CFR part 63 of appendix A. 

(b) When a flare is used to comply 

with § 63.126(b)(2), the owner or 

operator shall comply with the flare 

provisions in §63.11 of subpart A of this 

part. " :-,•••. 

(1) The compliance determination 

required by § 63.6(g) of subpart A of this 

part,a shall be conducting using 

Method 22 of 40 CFR part 60, appendix 

A, to determine visible emissions. The 

observation period shall be at least 2 

hours and shall be conducted according 

to Method 22. : r ': 

(i) The compliance determination 

shall be conducted during at least three 

complete loading cycles with a separate 

test run for each loading cycle. The 

observation period for detecting visible 

emissions shall encompass each loading 

cycle. 

(ii) Integrated sampling to measure > 

vent stream flow rate shall be performed 

continuously during each loading cycle. 

(2) An owner or operator is not 

required to conduct a performance test 

to determine the percent emission 

reduction or outlet HAP or TOC 

concentration when a flare is used. 

(c) An owner or operator Is not 

required to conduct a performance test 

when any device specified in 

paragraphs (c)(1). (c)(2), (c)(3); or (c)(4) 

of this section is used. 

"The EPA will propose tubpart A In the future. 

"See Footnote 11. 
P.4 

Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 /Corrections 11669 

(1) A boiler or process heater with a 

design heat input capacity of 44 

megawatts or greater. 

(2) A boiler or process heater burning 

hazardous waste for which the owner or 

operator: 

(i) Has been issued a final permit 

under 40 CFR part 270 and complies -

with the requirements of 40 CFR part 

266 subpart H, or 

(ii) Has certified compliance with the 

interim status requirements of 40 CFR 

part 268 subpart H. 

(3) A boiler or process heater into 

which the vent stream is introduced 

. with the primary fuel. 

(4) A vapor balancing system, 

(d) An owner or operator using a 

combustion device followed by a 

scrubber to control a halogenated 

transfer vent stream in compliance with 

§63.126(d) shall conduct a performance 

test to determine compliance With the 

control efficiency or emission limits for 

hydrogen halides and halogens. 

(1) For an owner or operator 

determining compliance with the 99 

percent reduction of total hydrogen 

halides and halogens, sampling sites -

shall be located at the inlet and outlet 

ofthe scrubber. For an owner or 

operator complying with the 0.5 

milligram per dry standard cubic meter 

outlet emission: limit for each hydrogen 

halide and halogen, the sampling site 

shall be located at the outlet of the 

scrubber. 

(2) Except as provided in paragraph 

(d)(5) of this section, Method 26 or 26A 

,- of part 60. appendix A, shall be used to 

determine the concentration in 

milligrams per dry standard cubic 

meter, corrected to a 3 percent oxygen 

oasis, of the hydrogen halides and 

halogens that may be present in the 

stream. 

(3) To determine compliance with the 

99 percent emissions reduction limit, 

the emissions for any hydrogen halides 

and halogens present at the scrubber 

inlet shall be summed together. The 

mass emissions of the compounds 

present at the scrubber outlet shall be 

summed together. Percent reduction 

shall be determined by comparison of. 

the summed inlet and outlet 

measurements. . - . 

(4) To demonstrate compliance with 

the 0.5 milligram per dry standard cubic 

meter emission limit, the test results 

must show that the concentration of 

each individual compound measured at 

the scrubber outlet, corrected to 3 y 

percent oxygen, is below 0.5 milligram 

per dry standard cubic meter or is below 

detectable levels. 

(5) The owner or operator may use 

any other method or data to demonstrate 

compliance if the method or data has 

been validated according to the protocol 

of Method 301 of 40 CFR part 63, 

appendix A. 

le) The owner or operator shall 

inspect the vapor collection system and 

vapor balancing system for detectable 

emissions greater than 500 parts per 

million. 

(1) Method 21 of 40 CFR part 60, 

appendix A and visual inspections shall 

be used. ^ y 

(2) Inspections shall be performed,. 

only while a tank truck or railcar is .••_ 

being loaded. 

'- (3) Inspections shall be performed at 

the following times: 

(i) By the compliance date and 

annually thereafter to demonstrate 

compliance with § 63.126(a)(3) and (4), 

or (b)(3); and .,..-. 7 . 

(iij Before each performance test 

required to demonstrate compliance 

with §63.126(b)(1).'ZZ'YY. .Y'YY... .YY YY 

(0 For the purposes of demonstrating 

vapor tightness to determine 

compliance with § 63.126(e)(2), the 

following procedures and equipment . 

shall be used: 

(1) The pressure test procedures 

.specified in Method 27 of part 60, . 

appendix A; and 

(2) A pressure measurement device 

which has a precision of ±2.5 

millimeters of mercury and which is. 

capable of measuring above the pressure 

at which the tank truck or raiicar is to 

be tested for vapor tightness. 

§63.131 Process wastewater provisions— 

flow diagrams and tables. . -.., 

(a) The flow diagrams in this section, 

are provided as guidance for 

understanding the basic 

interrelationships of the wastewater 

provisions' for process units' at new and 

existing sources. Paragraphs (a)(1) 

through (a)(8) of this section briefly 

outline the flow diagrams provided. 

(1) Figure 1 provides an overview of 

the HON wastewater provisions, 

(2) Figure 2 outlines the process for 

determining whether a stream meets the 

HON definition of a process wastewater 

stream, . .'.'.'.'•...''" •"'. " '-. 

• (3) Figure 3 summarizes Group 1 and 

Group 2 determinations for wastewater 

streams containing Table 8 HAP's, 

(4) Figure 4 summarizes Group 1 and 

Group 2 determinations for wastewater 

streams containing Table 9 HAP's, 

(5) Figure 5 summarizes compliance 

options for control of wastewater 

streams containing Table 8 HAP's, 

(6) Figure 6 summarizes compliance 

options for control of wastewater 

streams containing Table 9 HAP!s, 

(7) Figure 7 presents the process unit 

alternative compliance option for 

control of wastewater streams at existing 

sources containing Table 9 HAP's, and 

(8) Figure 8 outlines compliance 

options for control of residuals. 

(b) Because the flow diagrams are 

intricately related to Table 8 and Table 

9 and for easy reference, these two 

tables are also included in this section. 

BIUTJNO COD E 7IS<*-OI-O '.'•.'•'•." • 
P.5 

• * . . 

11670 Federal Register 7 Vol. 58, No. 37 /'Friday, February 26, 1993 /Corrections 

• 

Yes 

Control 

(Figure; »5.&8) 

. • . 

Figure 1 .Overview of HON Wastewater Provisions 
P.6 

Federal Register / Vol. 58,, No. 37 /Friday, February 26, 1993 / Corrections 11671 

Figure 2. HON Wastewater Determination 
P.7 

11672 Fed;^/Reg^f;/^:yol.h5Q;'..NpX 37./ Friday, February 26, 1993 /. Corrections 

Do fbr each wastewater stream 

generated from a process unit at a new source 

Determine Concentration 

and Flow Rate 

Flowrate &0.02 fpm ^s ^ No 

and Concentration of any 

Table 8 HAP 

alOppmw? 

Group 1 Wastewater Stream: 

Requires Treatment for Table 8 HAP's 

Go to Figure 5 

Figure 3. Group 1 and Group 2 Determinations for Wastewater Streams 

Table 8 HAP's (Refer to §63.132(c)) 
P.8 

Federal Register /Vol. 58, No. 37,/;,Friday; February 26, 1993 /Corrections 11673 

Do for each wastewater stream 

Determine Concentration 

and Flow Rate 

(§63.132(1)) 

Total 

VOHAP Concentration; 

21000 ppmw and Flow Rate 

alOjepm? 

••(§63.132(0(1)0)-

Group 2 

(Wastewater) 

Stream 

Yes Yes 

Group 2 

(Wastewater) 

Stream 

4. Group 1 and Group 2 Determinations for Wastewater Streams 

Table 9>IAP's (Refer to §§63.132(f) and 63.138(c)) g 
11674 i * • YU 7I^e^7Rjegistei^/5Volv;58;sNo/37 ^Friday;:Fe^ 

P.9 

Control Air Emissions Before 

and During Treatment/Recycle 

For One Group 1 '','"•'; 

Wastewater Stream Only: '•'-• 

One or 

No ^''"More Group 1 and/or\ ^ Yes 

J3roup 2 Wastewater Streams^ 

Combined? 

1 > Recycle to Process. : 7. .• : 

or 

2. Use Design Steam Stripper 

or • 

3. Reduce VOHAP Mass by.99% 

o r . ;:-

;"7 • 

4. : Reduce Concentration of Each 

HAPto <10ppmw' 7 :, n,...Y 

y.;-~-.;h'vCi -•?•• 

For One or More GroiTip 1/ 

Group 72 Wastewater Streams: 7. 

1. Recycle to Process.^;: 7 ^;;>v:~ yv 

..' ..-.'-or -Y.YY'ZYY '..'..,'.'.'••..••''•.' 

2. Use Design.Steam.Stripper.'; 

• •."or""':-.;' -" •' ""',':: y 

3. Reduce VOHAP Mass7 by 99% y 

•or' , ;••• . '"'y<,.y" 7 

4. ..Treat to Achieve Required 

. Mass Removal : ry 

Treat Residuals 

(Figured) 

{Determine if Group 11 

fbr Table 9 HAP's 

(Figure 4) 

Figure5. ComplianceQptibnsforControliofTable;8• HAP'stfr§63? U-iYS. 

s'A.vVi- -M-wV '"'•'•• '••;;•.••:! 
Federal Register /Vol. 58, No. 37 / Friday, February 26, 1993 /Corrections 

P.10 

11675 

Control Air EmissionsBefore 

and During Treatment/Recycle 

For One or More Individual 

Group 1 Wastewater Streams: 

1 Recycle to Process 

or 

2. Use Design Steam Stripper 

or 

3. Reduce VOHAP Mass by 

Percentages Specified for 

Strippabiirty Groups in Table 9 

or 

4. Reduce Total VOHAP Concentration 

to<50ppmw 

or 

5. Reduce VOHAP Mass by 99% 

For One or More Group 1/ 

Group 2 Wastewater Streams: 

1. Recycle to Process 

. o r 

2. Use Design Steam Stripper 

or 

3. Reduce VOHAP Mass by 

Percentages Specified for 

Strippabiirty Groups in Table 9 

or 

4. Treat to Achieve Required 

Mass Removal 

or 

5.. Reduce VOHAP Mass by 99% 

Figure 6, Compliance Options for Control of Table 9 HAP's 

•.'."•• (Refer to §63.138(c)) 
p.11 

11676 Federals Register ./.Voli 58;. No 37-7 Friday, February: 26;-: 1993 /Corrections 

For control of Table 9 HAP's onty 

Non-process wastewater streams and 

wastewater streams from other process 

units cahno» be combined when using this option 

Control Air Emissions Before 

and During Treatment/Recycle 

Ail Process Wastewater Streams 

from a Process Unit Must Comply 

with these Provisions if this 

Option is Selected 

For All Wastewater Streams; 

Recycle to the Process 

or 

Reduce Total VOHAP Concentration 

to < 10 ppmw before Being 

Discharged or Combined with 

Wastewater Streams from Other 

Process Units 

Figure 7, Process Unit Alternative Compliance Option 

(Refer to§63.138(d))

 : 
P.12 

Federal Register / Vol., 58, No. 37 / Friday, February 26, 1993 / Corrections 11677 

Control Air Emissions Before 

and During Treatment/Recycle 

For All Residuals: 

1. Recycle to Process 

(includes sale as feedstock) 

or 

2. Return to Treament Process 

or 

3. Destory Total HAP Mass by 99% 

(includes sale for energy recovery) 

Figure 8. Compliance Options for Control of Residuals 

(Refer to §63.138(g)) 

s 

s 

BtUINO CODE IMS-Ot-T 
P.13 

11678 Register /Vol. 58, No. 37 / Friday, February 26, 19,93 /Corrections 

\ 

TABLE 8.—ORGANIC HAP COMPOUNDS 

SUBJECT TO REQUIREMENTS FOR PROCESS UNITS AT NEW SOURCES 

Chemical name 

Ally) chloride 

Benzene 

1,3-Butadlene 

Carbon disulfide 

Carbon tetrachloride ....-

Cumene (isopropyl benzene) 

Ethylbenzene 

Ethyl chloride (Chloroethane) 

Ethylidene dichloride (1.1-

Dichkxoethane) -

Hexachlorobutadiene 

Hexachloroethane 

Hexane 

Methyl bromide (Bromomelhane) ... 

Methyl chloride (Chtoromethane) ... 

Methyl chloroform (1,1,1-

Trichloroethane) 

Phosgene 

Tetrachloroethylene 

(Perchloroethylene) 

T

oluene 

T

richloroethylene ...7 

2.2.4-Trimethylpentane 

Vinyl chloride ; 

Vinylidene chloride (1,1-

Dichlorosthytene) .. 

nvXylene 7 

p-Xylene : '. : 

CAS 

numbe*0 

107051 

71432 

106980 

75150 

56235 

98828 

100414 

75003 

75343 

87683 

67721 

110543 

74839 

74873 

71556 

75445 

127184 

108883 

79016 

540841 

75014 

75354 

108383 

106423 

"CAS numbers refer to the Chemical 

Abstracts Service registry number assigned to 

specific compounds, isomers, or mixtures of 

compounds. 

TABLE 9.—ORGANIC HAP STRIPPABILITY 

GROUPS AND TARGET REMOVAL EFFICIENCIES 

Strippability 

group 

A 

B 

C 

Compound name 

See attached list 

of compounds. 

See attached Ust 

of compounds. 

See attached list 

of compounds. 

Target removal efficiency 

(percent) 

99 

95 

70 

Strippability 

group 

A 

Compound name 

Acetaldehyde ..7.... 

Allyl chloride 

Benzene -.;... 

Benzyl chloride .... 

1,3-Butadiene 

Carbon disulfide .. 

Carbon tetra-

. chloride. 

Chlorobenzene .... 

Chloroform 

Chloroprene (2-

Chk>ro-1,3-Butadiene). 

CAS number" 

75070 

107051 

71432 

100447 

92524 

75252 

106990 

75150 

56235 

108907 

67663 

126998 

Strippability 

group Compound name 

Cumene (isopropyl benzene). 

1.4-Dichtorobenzene(p). 

1,3-Dichtoropropene. 

Ethvlbenzene 

Ethyl chloride 

(Chloro- ethane). 

Ethylene 

dibromide. 

Ethylene dichloride (1,2-

Dichloro-eth- . 

ane). 

Ethylene oxide 

Ethylidene dichloride (1,1-

Dtchloro- ethane). 

Hexachloro- benzene. 

Hexachloro- butadiene. 

Hexachloro- ethane. 

Hexane 

Methyl bromide 

(Bromo-methane). 

Methyl chloride 

(Chloro- meth-

• ane). 

Methyl chloroform 

(1.1.1-Trichloro- ethane). 

Methyl ethyl ketone (2-

Butanone). 

Methyl isobutyl ketone (Hexone). 

Methyl terl-butyl 

ether. 

Methylene chloride (Dichloromethane). 

Naphthalene : 

2-Nitropropane 

Phosgene 

Propylene dichloride (1.2-

Dtchloro- propane). 

Propylene oxide... 

Styrene 

1.1.2.2-

Tetrachloroe thane. 

Tetrachloro-ethylene (Perchloroethylene). 

Toluene 

1.2.4-Trichtorobenzene. 

1.1,2-Trichloroethane. 

Trichloro- ethylene 

Triethylamine 

2,2.4-Trimethylpentane. 

Vinyl acetate 

Vinyl chloride 

CAS number0 

98828 

106467 

542756 

100414 

75003 

108934 

107062 

75218 

75343 

118741 

87683 

67721 

110543 

74839 

74873 

71556 

78933 

108101 

1634044 

75092 

91203 

79469 

75445 

78875 

75569 

100425 

79345 

127184 

108883 

120821 

79005 

79016 

121448 

540841 

108054 

75014 

Strippability 

group 

B 

C 

Compound name 

Vinylidene chloride. 

(1.1-DfcNoroethylene). 

m-Xytehe ..... 

o-Xylene 

Acetonltrile -

Acetopheriohe 

Acrolein 

Acrylonitrile 

2-ChSoroacetophenone. 

Dichtoroethyl ether 

N,NrOimethy»-anlline. 

2,4-Dlnitro-phencJ 

Ethylene glycol dimethyl ether. 

Ethylene glycol 

mono-butyl 

ether acetate. 

Isophorone 

Methyl methacrylate. 

Propionalde-hyde 

2,4,5-Trichlorophenol. 

Aniline 

o-Cresol 

Diethyl sulfate 

3,3'-Dimethyl-benzidihe. 

1,1-Dime thyl-hydrazine. 

Dimethyl sulfate ... 

2,4-Dinitro-toluene 

1,4-Dioxane (1,4-

Di- ethyleneoxide). 

Epichloro-hydrin. 

(1-Chloro-2.3-

epoxy- propane). 

Ethylene glycol 

mono-methyl 

ether acetate. 

Diethylene glycol 

diethyl ether. 

Diethylene glycol 

dimethyl ether. 

Ethylene glycol 

mono-ethyl 

ether acetate. 

Methanol 

o-ToiuJdine 

CAS number" 

75354 

108383 

95476 

106423 

75058 

98862 

107028 

107131 

532274 

111444 

121697 

51285 

140885 

110714 

112072 

78591 

80626 

98953 

123386 

95954 

62533 

95487 

64675 

119937 

57147 

77781 

121142 

123911 

106898 

110496 

112367 

111966 

111159 

67561 

95534 

. "CAS numbers refer to the Chemical 

Abstracts Service registiy number assigned to 

specific compounds, isomers, or mixtures, of 

compounds. ' 

§ 63.143 Process wastewater jwovlolcno— 

bispocilcno ond monitoring ot operationa 

(a) For each wastewater tank, surface 

impoundment, container, individual 

drain system, and oil-water separator 

that receives, manages, or treats a Group 

1 wastewater stream or residual 

removed from a Group 1 wastewater 

stream, the owner or operator shall 
P.M 

Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 11679 

comply with the 

inspectionrequirements specified in 

Table 10 of this subpart. 

to. comply with 

Tanks: 

63.133(bKD(H) ~. 

63.133(c) 

63.133(d) 

63.133(e) _.. 

Surface impoundments: 

63.134(bM1)(U) '... 

63.134(c) „ 

Containers: 

63.135(b)(2) ; 

63.135(d)(2) 

63.135(e) - „ 

Individual drain systems.*: 

63.136(b)(1)(H) 

63.136(b)(3) „ 

63.136(c)(1) ............_„ 

63.136(c)(4)(l) - , 

63.136(c)(4)(H) 

63.l36(c)(4)(Hi) '. 

Oil-water separators: 

63.137(b)(1)(H) •• —... 

63.137(c)....„_ 

j . « 

63.137(d) 

TABLE 10.—MONITORING REQUIREMENTS FOR WASTE MANAGEMENT UNITS 

Inspection or monitoring requirement 

Inspect fixed roof and all openings tor leaks0 ..... 

Inspect floating roof in. accordance with 

§§63.120(a)(2) and (a)(3). 

Measure floating roof seal gaps In accordance 

with §§63.120(b)(2)(i) through (b)(6)(H). 

—Secondary seal gaps -

Inspect wastewater tank for failures and Improper work practices. 

Inspect cover and all openings for leaks0 

Inspect surface impoundment for failures and 

improper work practices. 

Inspect enclosure and all openings for leaks".... 

Inspect container for failures and improper work 

practices. 

Inspect cover and aO openings for leaks0 ,. 

Inspect individual drain system tor failures and 

i improper work practices. 

Verify flow of water supply to all drains using 

:water seals to ensure appropriate water levels 

.and to prevent other conditions that reduce 

water seal control effectiveness. 

Inspect all drains using tightly-sealed caps or 

plugs to ensure caps and plugs are In place 

and properly installed. 

Inspect all junction boxes to ensure covers are 

in place and have tight seals around edges. 

Inspect unburied portion of all sewer lines for 

cracks and gaps. 

Inspect fixed roof and aH openings for leaks" ..... 

Measure floating roof seat gaps bt accordance 

with 40 CFR 60.696(d)(1). ; 

-Primary seal gaps ; 

—Secondary seal gaps 

Inspect oil-water separator for failures and improper work practices. 

Frequency 

-AftftUfiltV MMM* M..M.M. MM ..... ... 

See §63.120('al('27a^ (a)(3) 

Once every 5 years. 

Annually. 

Semi-annually 

Annually 

Semi-annually 

Annually 

Annually 

Semi-annually „ 

Semi-annually: 

Semi-annually 

Semi-annually 

Once every 5 years. 

Annually. . 

Semi-annually ; 

-

Method 

Method 21 b. 

Visual. 

See § 63.120(b)(2)(H) through 

(b)(6)(H) 

Visual. 

Mathod 21 •». 

Visual. 

Method 21 b. 

Method 21". 

Visual. 

Method 21". 

Visual. 

Visual. 

Visual. 

Visual. 

Method 21 b 

See40CFR60.686(dX1). 

Visual. 

" Leaks are detectable emissions of 500 parts per million by volume above background. 

•"Method 21 of 40 CFR Part 60, Appendix A. 

cAs specified In §63.136(a), the owner or operator shall comply with the requirements of either §363.136 (b) or (c). 

(b) For each waste management unit or treatment process used to comply with § 63.138(b)(1), (c)(1), or (d) of this 

subpart, the owner or operator shall comply with the monitoring requirements specified in Table 11 of this subpart. 

. To comply wtth 

1. Effluent totaJ VOHAP average concentration: 63.138-

(c)(1)(H)(C) 63.138(d)(2)(i). 

TABLE 11.—MONITORING REQUIREMENTS FOR TREATMENT PROCESSES 

Parameters to be monitored 

A. Measure effluent total VO concentration as a 

surrogate for VOHAP concentration, or 

B. Measure effluent total VOHAP concentraSon 

Frequency 

Monthly „:.„.i..„.„.i„...„„.4 

Methods 

Method 25D 

Proposed Mathod 305, or 

any other appiicabie method which has been validated using section 5.1 or 

5.3 of Method 301 ° 
11680 Federal; Register. / Vol. 58, No; 37 / Friday* February 26, 1993 / Corrections 

TABLE 11.—MONITORING REQUIREMENTS FOR TREATMENT PROCESSES—Continued 

To comply with 

2. Effluent VOHAP concentration of each HAP: 63.138-

(b)(1)(H)(A):; ; 

3. Percentage reduction of 

total VOHAP mass f}ow 

rate: 63.138(c)(1)(ii)(B); 

63.138(c)(1)fiH)(B). 

4. Percent reduction: df 

VOHAP mass flow rate for 

each strippability group ' of 

HAP's: 63.138(b)(1)(H)(C) 

63.138(b)(1)(Hi)(A) 

63.138(c)(1)(H)(D) 63.138-

(c)(1)(iii)(C). 

5. VOHAP mass removal of: 

HAP's In a treatment process other than a properly 

operated biological treatment unit 63.138(b)(1)(Hi)(C): 

6. VOHAP. mass removal of 

total HAP's In a treatment 

process other than a property operated biological 

treatment unit 

. 63.138(c)(1p)(D). ; ' 

7. VOHAP mass removal of 

each or total HAPs ih a 

properly operated biological 

treatment unit 63.138(b)(1)-

f.ii)(C) 63.138(c)(1)(ifl)(D), .: 

8. Altemative to items 1 

through 7 above. 

9. Design steam stripper 

63.138(f)(3), (4). (5). and (6). 

Parameters to be monitored 

Measure VOHAP concentration of each HAP 

A. Measure total VO concentration as a surrogate for VOHAP concentration In influent and 

7 effluent, or

 ;

 -' 

B. Measure total VOHAP concentration In Influent and effluent 

A. Measure: VOHAP concentration of each 

strippability group of HAP's In influent and effluent or • 

B. Measure concentrations of speciated HAP's 

In Influent and effluent 

A. Measure VOHAP concentration of each HAP 

in influent and effluent of treatment process or 

treatment process train, or 

B. Measure concentrations of speciated HAPs 

in influent and effluent of treatment process or 

treatment process train 

Measure total VOHAP concentration In Influent 

and effluent of treatment process or treatment 

process train

 v ; 

Appropriate parameters may be monitored upon 

approval from the Administrator in accordance 

with ihe requirements specified in §63.143(c) 

Other parameters may be monitored upon approval from the Administrator in accordance 

with the requirements specified Ih § 63.143(d) 

Steam flow rate ......:.............:...... .....Y......... 

Wastewater feed mass flow rate ......... 

Wastewater feed temperature 

> 

Condenser vapor outlet temperature .................. 

Frequency 

Monthly „ ; .... 

Monthly .: ;..... 

Monthly ..;......... ,..„....,„ 

Monthly; •i;.:..i..:.±.L.^.^..:.; 

Monthly: .......;.......... 

Mdntt5ly;.;..:....:..;„....;,:..„...L 

Monthly......v..:.......;.;..;;.:.„..;;/ 

. MonthVC.„....-7;.:...:.......:....: 

Monthly ..........;.....;.„;J..;..v.;... 

Continuously ...........7..;..' 

Continuously ...........7„.,..„ 

Continuously ..;.....i.,......U..;;. 

Continuously ..;.....:.,;.;...-..:;:„. 

•If method(s) are used to measure organic HAP concentrations bi''a waste or wastewater stream; ral 

concentrations In an air stream purged from a waste or wastewater stream, the. correction factors listed In Table 

results to provide a measure of the volalfle portion Oe.. the VOHAP concentratlbn) of the organic HAP's. 

Methods 

Proposed Method 305, or 

any other applicable method which has been validated using section 5.1 or 

5.3 of Method 301» 

Method 25D 

Proposed- Method 305, or 

: any other, applicable meth-

; od which has been validated using section 5.1 or 

• 5.3 of Method 301 • -

Proposed Method 305, or 

any other applicable'method which has been validated using section 5.1 or 

5.3 of Method 301 \ 

Any applicable method which 

has • been validated using 

: section 5.1 or 5.3 of Method 301 ' • • ..";-: y 

Proposed. Method 305, or 

any other applicable meth-

. od which has been vall-

• dated using section 5.1 br 

5.3 of Method 301 • 

Any appiicabie method which 

has been validated using 

section 5.1 or 5.3 of Meth-

.'• ,od.30ir; :.•'• 

Proposed' Method 305, or 

any other applicable meth-

•, ' bd; which jias been vall-; 

i dated using Section 5.1 or 

5.3 of Method 301 \ 

Method 304, or any other 

method which has been 

approved by EPA during 

compliance: ,:• demonstra-

- tions ; , 

Integrating steam flow mon-

• • itoring 'device •• equipped 

with a continuous recorder 

Uquld flow meter installed at 

stripper:. - influent' and; 

, equipped with a-contlnu-

"' ; bus recorder* Y '• Y Y" ."• 

• Lkjuid;.temperature -monitorl; ..ing .device J Installed at 

7 stripper Influent and 

; equipped with a i continuous recorder ;-. 

Temperature monitoring device Installed at condenser 

vapor outlet and equipped 

with a continuous recorder 

her than measuring VOHAP 

13 may be used to adjust the 

P.15 

> 
P.16 

Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 11681 

(c) If the owner or operator elects to 

comply with Item 7 in Table 11 of this 

subpart, the owner or operator shall 

request approval to monitor appropriate 

parameters that demonstrate proper 

operation ofthe biological treatment 

unit. The request shall be submitted 

according to the procedures specified in 

§ 63.146(a)(3) and in either § 63.151(f) or 

§ 63.152(e) of this subpart. 

(d) If the owner or operator elects to 

comply with Item 8 in Table 11 of this 

subpart, the owner or operator shall 

request approval to monitor parameters 

other than those listed in Items 1 

through 7 of Table 11. The request shall 

be submitted according to the 

procedures specified in § 63.146(a)(3) 

and in either § 63.151(f) or § 63.152(e) of 

this subpart, and shall include a 

description of planned reporting and 

recordkeeping procedures. The 

Administrator will specify appropriate 

reporting and recordkeeping 

requirements as part ofthe review of the 

Implementation Plan or permit 

application. 

fe) Except as provided in paragraphs 

(e)(4) and (e)(5) of this section, for each 

closed vent system and control device 

used to comply with the requirements of 

§§63.133 through 63.139 of this 

subpart, the owner or operator shall 

comply with the requirements in 

§ 63.139(e), (f), and (h) of this subpart, 

and with the requirements specified ix. 

paragraph (e)(1), (e)(2), or (e)(3) of this 

section. 

(1) The owner or operator shall 

comply with the monitoring 

requirements specified in Table 12 of 

this subpart; or 

Control device 

All control devices :.. 

Thermal incinerator 

Boiler or process heater <44 

megawatts and vent stream 

is not mixed with the primary fuel. 

Carbon adsorber (regenerative). 

Carbon adsorber (non-regenerative). 

TABLE 12.—MONITORING REQUIREMENTS FOR CONTROL DEVICES 

Monitoring equipment required 

1. Flow indicator Installed at all bypass lines to 

the atmosphere and equipped with continuous 

recorder6 or. 

2. Valves sealed ciosed with car:seal or lockand-key configuration. 

Temperature monitoring device installed in firebox or in ductwork Immediately downstream 

of firebox * and equipped with a continuous re^ 

corder6. 

Temperature monitoring device installed in gas 

stream immediately before and after catalyst 

bed and equipped with a continuous recorder6

. 

Heat sensing device installed at the pilot light 

and equipped with a continuous recorderb. 

Temperature monitoring device installed in firebox* and equipped with continuous recorder6

. 

Temperature monitoring device Installed at condenser exit and equipped with continuous recorderb

. 

Integrating regeneration stream flow monitoring 

device having an accuracy of ±10 percent and 

equipped with a continuous recorder6, and. 

Carbon bed temperature monitoring device 

equipped with a continuous recorder6. 

Organic compound concentration monitoring device0

. 

Parameters to be monitored 

1. Presence of flow diverted 

from the control device tb 

the atmosphere or. 

2. Monthly inspections of 

sealed valves. 

• ; 

Temperature upstream and 

downstream of catalyst 

bed.. 

Presence of a flame at the 

pilot Ught. 

Combustion temperature 

Condenser exit (product 

side) temperature. 

Total. regeneration stream 

mass flow during carbon 

bed regeneration cyde(s).: 

Temperature of carbon bed 

after regeneration (and 

within 15 minutes of completing any cooling 

cycle(s)] and duration of 

the carbon bed steaming 

cycle. 

Organic compound concentration of adsorber exhaust . 

Frequency 

Continuous 

Monthly 

Continuous 

Continuous 

Continuous 

Continuous 

-

Continuous 

Continuous 

3 •• • •• -

Continuous . . 

,, 

DaUy or at intervals no greater than 20 percent of the 

design carbon replacement 

interval, whichever Is 

greater 

* Monitor may be installed in the firebox or in the ductwork Immediately downstream of the firebox before any substantial heat exchange is 

encountered. 6

 "Continuous recorder" is defined in §63.111 of this Subpart 

c

 As an altemative to conducting this monitoring, an owner or operator may replace the carbon in the carbon adsorption system with fresh 

carbon at a regular predetermined time interval that is less than the carbon replacement interval that is determined by the maximum design flow 

rate and organic concentration in the gas stream vented to the carbon adsorption system. 

(2) The owner or operator shall use an 

organic monitoring device installed at. 

the outlet of the control device and 

equipped with a continuous recorder. 

Continuous recorder is defined in 

§ 63.111 of this subpart; or 

(3) The owner or operator shall 

request approval to monitor parameters 

other than those specified iri paragraphs '" 

(e)(1) and (e)(2) of this sectiori. The 

request shall be submitted according to 

the procedures specified in 

§ 63.146(a)(3) and in either § 63.151(f) or 

§ 63.152(e) of this subpart, and shall 

include a description of planned

 ; 

reporting and recordkeeping 

procedures. The Administrator will 

specify appropriate reporting and 

recordkeeping requirements as part of 
P.17 

11682 Federal Register,/ Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

the review of the Implementation Plan 

or permit application. 

(4) For a boiler or process heater in 

which all vent streams are introduced 

with primary fuel,'the owner or operator 

shall comply with the requirements in 

§ 63.139 (e), (f). and (h), but the owner 

or operator is exempt from the 

monitoring requirements specified in 

paragraphs (e)(1) through (e)(3) of this 

section. 

(5) For a boiler or process heater with 

a design heat input capacity of 44 

megawatts or greater, the owner or 

operator shall comply with the 

requirements in § 63.139 (e), (f), and (h), 

but the owner or operator is exempt 

from the.monitoring requirements 

specified in paragraphs.(e)(1) through 

(e)(3) of this section. 

(f) For each parameter monitored in 

accordance with paragraph (c), (d), or (e) 

of Uiis section, the owner or operator 

shall establish a range that indicates 

proper operation of the treatment 

process or closed vent system and 

control device. In order to establish the 

range, the information required in 

§ 63.152(b)(2) of this subpart shall be 

submitted in the Notification of 

Compliance Status or the operating 

permit application in accordance with 

the requirement specified in §§ 63.146 

(b)(6)(ii)(A) and (b)(7)(iii). 

(g) Monitoring equipment shall be 

installed, calibrated, and maintained 

according to the manufacturer's 

specifications. 

§ 63.144 Process wastewater provisionstest methods end procedureo to determine 

applicability. 

(a) An owner or operator shall 

determine the annual wastewater 

quantity for a wastewater stream by one 

of the following methods: 

(1) Selecting the highest annual 

quantity of wastewater managed from 

historical records representing the most 

recent 5 years of operation or, if the 

process unit at the source has been in 

service for less than 5 years but at least 

1 year, from historical records 

representing the total operating life of 

the source; 

(2) Using the maximum design 

capacity Ofthe waste management unit; 

(3) Using the maximum wastewater 

generation rate based on the maximum 

design production capacity ofthe 

process unit generating the wastewater 

stream; or 

(4) Measurements that are 

representative of maximum wastewater 

generation rates. 

(b) An owner or operator shall 

determine the total VOHAP average 

concentration or average VOHAP. 

concentration of each HAP for the point 

of generation of each wastewater stream 

by one of the following methods: 

(1) Knowledge ofthe wastewater. Tfie 

owner or operator shall provide 

sufficient infonnation to document the 

total VOHAP average concentration or 

average VOHAP concentration of each 

HAP of each wastewater stream. 

Examples of information that could 

constitute knowledge include material 

balances, records of chemicals 

purchases, process stoichiometry, or 

previous test results provided the 

results are still representative of current 

operating practices at the process 

unit(s). If test data are used, then the 

owner or operator shall provide 

documentation describing the testing 

protocol and the means by which 

sampling variability and analytical 

variability were accounted for in the 

determination ofthe total VOHAP 

average concentration or average 

VOHAP concentration of each HAP for 

the wastewater stream. 

(2) Bench-scale or pilot-scale test data. 

The owner or operator shall provide 

sufficient information to demonstrate 

that the bench-scale or pilot-scale test 

concentration data are representative of 

the actual total VOHAP average 

concentration or average VOHAP 

concentration of each HAP. The owner 

or operator shall also provide 

documentation describing the testing 

protocol, and the means by which 

sampling variability and analytical 

variability were accounted for in the 

determination of total VOHAP average 

concentration or average VOHAP 

concentration of each HAP for the 

wastewater stream. 

(3) Measurements made at the point of 

generation or, when not feasible, 

measurements made at a downstream 

location that are corrected to point of 

generation values of the total VOHAP 

average concentration or average 

VOHAP concentration of each HAP in 

the wastewater stream in accordance 

with the following procedures: -

(i) Collect a minimum of three 

samples from each wastewater stream 

which are representative of nonnal flow 

and concentration conditions. Where 

feasible, samples shall be taken from an 

enclosed pipe prior to the wastewater 

being exposed to the atmosphere. 

Wastewater samples shall be collected 

u&jng the sampling procedures specified 

in 40 CFR part 60, appendix A, Method 

25D. 

(ii) When sampling from an enclosed 

pipe is not feasible, a minimum of three 

representative samples shall be 

collected in a manner to minimize 

exposure of the sample to the 

atmosphere and loss of HAP compounds 

prior to sampling. 

(iii) Each wastewater sample shall be 

analyzed using one of the following test 

methods for determining the total 

VOHAP average concentration or 

average VOHAP concentration of each 

HAP in e wastewater stream: 

\ (A) For total VOHAP average 

concentration or average VOHAP 

concentration of each HAP, proposed 

Method 305 shall be used. TTie target 

components shall be stripped from the 

wastewater samples using the 

procedures specified in proposed 

Method 305 (i.e., suspended in a 

polyethylene glycol/water matrix, 

heated to 75 °C, purged with 6 liters per 

minute pf gaseous nitrogen, sampled for 

30 minutes, etc.). The exiting purge 

stream containing the target components 

shall be collected and analyzed using 

the appropriate techniques described in 

proposed Method 305. The precision 

and accuracy requirements of proposed 

Method 305 must be met as part of the 

compliance requirements of this rule. 

Performance audit samples, if available, 

shall be analyzed using the procedures 

specified in proposed Method 305. 

The following equation shall be used 

to calculate the VOHAP concentration 

ofan individually-speciated compound 

in the wastewater from the proposed 

Method 305 result: 

24.055 760 

x xtxLxlO3 )/Ms 
P.18 

er / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

where: 

Cw=VOHAP concentration ofthe 

individually-speciated HAP 

compound in the wastewater, parts 

per million by weight. 

Cc=Concentration of compound in the 

gas stream, as measured by 

proposed Method 305, parts per 

million by volume on a dry basis. 

Ms=Mass of sample, from proposed 

Method 305, milligrams. 

MW=Molecular weight of the HAP 

compound, grams per gram-mole. 

24.055=Ideal gas molar volume at 293 

"Kelvin and 760 millimeters of 

mercury, liters per gram-mole. 

Pi=Barometric pressure at the time of 

sample analysis, millimeters 

mercury absolute. 

760=Reference or standard pressure, 

millimeters mercury absolute. 

293=Reference or standard temperature, 

"Kelvin. 

T;=Sample gas temperature at the time 

of sample analysis, "Kelvin. 

t=Actual purge time, from proposed 

Method 305, minutes. 

L=Actual purge rate, from proposed 

. Method 305, liters per minute. 

103=Conversion factor, milligrams per 

gram. 

Total VOHAP average concentration can 

be determined by summing the VOHAP 

concentrations of all HAP compounds 

in the wastewater. 

(B) Method 25D of part 60, appendix 

A may be used instead of proposed 

Method 305 to measure total VO average 

concentration as a surrogate for total 

VOHAP average concentration; 

(C) A test method or results from a 

test method that measures organic HAP 

concentrations in the wastewater, and 

that has been validated according to 

section 5.1 or 5.3 of Method 301 of 

appendix A of this part may be used. 

The specific requirement of proposed 

Method 305 to collect the sample into 

polyethylene glycol would not be 

applicable. The concentrations ofthe 

individual organic HAP compounds 

measured in Uie water may be corrected 

to their concentrations had they been 

measured by proposed Method 305, by 

multiplying each concentration by the 

compound-specific fraction measured 

factor in Table 13 of this subpart. 

TABLE 13.—FRACTION MEASURED (F,») 

AND FRACTION EMITTED (Fe) FOR HAP 

COMPOUNDS IN WASTEWATER STREAMS 

Chemical Warns 

Acetaldehyde 

Acrolein 

Fm 

0.724 

0.739 

0.807 

0.850 

0.875 

F. 

0.469 

0.354 

0.302 

0.445 

0.457 

TABLE 13.—FRACTION MEASURED (Fm) 

AND FRACTION EMITTED (Fe) FOR HAP 

COMPOUNDS IN WASTEWATER 

STREAMS—Continued 

Chemical Name 

Allyl chloride . ... „. 

AnBin® . ;~. 

Benzyl chloride .. ......... 

1,3-Butadiena 

Carbon disulfide 

2-Chleroacetophertone ..... 

Chloroform 

Chloroprene (2-Chloro1,3-6utadiene) 

Cumene (isopropyl benzene) 

1,4-Dich(oroben2ene(p).... 

1,3-Dlchloropropene 

Diethyl sulfate _ 

S.S'-Dimethylbenzldlne ..... 

1,1-Dimethylhydrazine 

2,4-DJnitrophenol 

2,4-Dtnitrotoiuene 

1,4-Dioxane (1,4-

Diethyleneoxlde) 

Epichlorohydrin(1-Chloro2,3-epoxy propane) 

Ethylbenzene 

Ethyl chloride 

(Chloroethane) 

Ethylene dichloride (1,2-

Dtchlorosthane) 

Ethylene oxide 

Ethylidene dichloride (1,1-

Dichloroethane) 

Diethylene glycol diethyl 

ether 

Ethylene glycol monobutyl 

ether acetate 

Ethylene glycol dimethyl 

ether 

Ethylene glycol monoethyl. 

other acetate ... 

Diethylene glycol dimethyl 

ether 

Ethylene glycol 

monomethyl ether acetate „ 

Hexachlorobenzene 

Hexachlorosthane 

Hexane 

Methanol 

Methyl bromide 

(Bromomsthans) „ 

Methyl chtorids 

(ChJoromethane) ........... 

Methyl chloroform (1,1,1-

TrtehJoroathane) 

Methyl ethyl ketone (2-

Butamms) ..... 

F„ 

1.000 

0.245 

1.000 

1.000 

1.000 

0.481 

1.000 

1.000 

1.000 

0.841 

1.000 

1.000 

1.000 

0.119 

1.000 

1.000 

0.939 

1.000 

1.000 

0.014 

0.110 

0.486 

0.077 

0.014 

0.004 

0.681 

0.859 

0.788 

1.000 

1.000 

1.000 

1.000 

0.712 

1.000 

0.770 

0.100 

0.680 

0.360 

0.370 

0.370 

1.000 

1.000 

1.000 

1.000 

0.997 

0.321 

0.539 

1.000 

1.000 

0.881 

F0 

0.755 

0.194 

0.721 

0.534 

0.550 

0.568 

0.888 

0.802 

0.832 

0.375 

0.698 

0.699 

0.604 

0.189 

0.777 

0.684 

0.358 

0.692 

0.329 

0.275 

0.233 

0.189 

0.247 

0.297 

0.231 

0568 

0.293 

0.459 

0.744 

0.772 

0.581 

0.619 

0.515 

0.722 

0506 

0.328 

0.389 

0.194 

0.184 

0508 

0.637 

0.761 

0.748 

1.000 

0.397 

0.278 

0.735 

0.751 

0.796 

0.475 

TABLE 13.—FRACTION MEASURED (Fm) 

AND FRACTION EMITTED (Fe) FOR HAP 

COMPOUNDS IN WASTEWATER 

STREAMS—Continued 

Chemica) Nam® 

Msffiyl isobutyl ketone 

Methyl tart-butyl ether 

Methylene chloride 

2-Nitropropane 

Phosgene 

Propylene dichtortde (15-

Dichloropropane) 

1,15.2-Tetrachloroethane 

Tetrachloroethylene 

Toluene 

o-ToMdine 

1,2,4-Trlchlorobenzene .... 

Trichloroethylene 

2,4,5-Trichlorophenol 

2,2,4rTrimethy!pentane .... 

Vinyl chloride 

Vinylidene chloride (1,1-

Dichloroethytene) 

• CJ 

0.954 

0.802 

0.911 

1.000 

1.000 

0.575 

0.537 

0.868 

0.813 

1.000 

0.841 

1.000 

1.000 

1.000 

1.000 

0:267 

1.000 

0.966 

1.000 

0586 

0.930 

1.000 

0.748 

1.000 

1.000 

1.000 

1.000 

1.000 

Fo 

0.547 

0.447 

0.570 

0.680 

0.561 

0.365 

0.469 

0.945 

0.424 

0.678 

0.541 

0.671 

0.518 

0.797 

0.731 

0.198 

0.652 

0.596 

0.761 

0598 

0.473 

1.000 

0.564 

0.823 

0.822 

0.740 

0.712 

0.740 

(iv) The total VOHAP average 

concentration or average VOHAP 

concentration of each HAP shall be 

calculated by averaging the results of 

the sample analyses as follows: 

_ l. n . 

C = —x l (Q0(Ci) 

Q.

 ,=1 

where: 

C=Total VOHAP average concentration 

or average VOHAP concentration of 

each HAP for wastewater stream, 

parts per million by weight. 

Q,=Total annual wastewater quantify for 

wastewater stream, kilograms per 

year. 

n=Number of wastewater samples (at 

least 3). 

Q=Annual wastewater quantify for 

wastewater stream represented by 

Q, kilograms per year. 

Q=Measured average concentration (i.e., 

total VOHAP average concentration 

or average VOHAP concentration of 

each HAP) in wastewater sample i, 

parts per million by weight. 

ii um\.mmmimmmm.mmm 
P.19 

11684 Federal Register / Vol. 58, No. 37 /Friday, February 26, 1993 / Corrections 

(c) To demonstrate that the total 

VOHAP mass flow rate from Group 1 

wastewater streams in new and existing 

SOCMI units is less than 1 megagram 

per year as specified in § 63.138(c)(5) of 

this subpart, an owner or operator shall 

determine for the'source the total 

VOHAP mass flow rate from all Group 

1 wastewater streams identified in 

§ 63.132(f)(1) of this subpart at their 

points of generation by the following 

procedure: 

(1) Determine the annual wastewater 

quantity for each wastewater stream 

using the procedures specified in 

paragraph (a) of this section. 

(2) Determine the total VOHAP 

average concentration for each 

wastewater stream using the procedures 

specified in paragraph (b) of this 

section. 

(3) Calculate the annual total VOHAP 

mass flow rate in each wastewater 

stream by multiplying the annual 

average flow rate 7of the wastewater 

stream times the total VOHAP average 

concentration. 

(4) Calculate the total source VOHAP 

mass flow rate from all Croup 1 

wastewater streams by adding together 

the annual total VOHAP mass flow rate 

from each Group 1 wastewater stream. 

(d) An owner or operator electing to " 

reduce the total source VOHAP mass 

flow rate tb less than 1 megagram per 

year in accordance with § 63.136(c)(6) of 

this subpart shall determine the total 

source VOHAP mass flow rate from 

Group 1 wastewater streams identified 

in § 63.138(f)(1) of this subpart by the 

following procedures: 

(1) The annual total VOHAP mass 

flow rate of each Group 1; wastewater 

stream treated to the level of the 

provisions of 63.138(c) of this subpart 

shall not be included in the total source 

VOHAP mass flow rate calculation. 

(2) For each untreated Group 1 

wastewater stream, annual total VOHAP 

mass flow rate shall be determined by 

the procedures iri paragraph (c) of this 

section. 

(3) For each Group 1 wastewater 

stream treated to levels less than 

required by the provisions of § 63.138(c) 

of this subpart, Uie annual total VOHAP 

mass flow rate shall be determined as 

follows: 

(i) Measurement pr sampling shall 

occur, at the point of discharge of the 

treatment process or series of treatment 

processes. The point of discharge is 

defined as the point-where the treated 

wastewater exits the treatment prbcess 

but before it is m^xed with other. 

wastewater streaiBs. and prior to 

exposure to the athiosphere. 

(ii) Determine the annual wastewater 

quantity for each wastewater stream at 

the point of discharge of the treatment 

process or series of treatment processes 

using the procedures specified in 

paragraph (a) of this section. 

(iii) Determine the total VOHAP 

average concentration fbr each 

wastewater stream at the point of 

discharge using the procedures 

specified in paragraph (b) of this 

section." 

(iv) Calculate the annual total VOHAP 

quantity in each wastewater stream by 

multiplying the annual wastewater 

quantity ofthe wastewater stream times 

the total VOHAP average concentration. 

(4) The total source VOHAP mass 

flow rate shall be calculated by 

summing the annual total VOHAP 

J

uantity from all wastewater streams as 

etermined in paragraphs (d)(2) and 

(d)(3) of this section. 

(e) Td determine the annual average 

wastewater flow rate for a wastewater 

stream, one ofthe following methods 

shall be used: 

(1) Use the maximum production 

capacity ofthe process unit, knowledge 

of the process, and mass balance 

information to either: estimate directly 

the average wastewater flow rate; or 

estimate the total annual wastewater, 

volume and then divide total volume by 

525,600 minutes in a year, 

(2) Select the highest average flow rate 

of wastewater from historical records ":" 

representing the most recent 5 years of 

operation or, if the process unit has 

been in service for less than 5 years but 

at least 1 year, from historical records 

representing the total operating life of 

the process unit; 

(3) Measure the flow rate of the 

wastewater for the point of generation 

during conditions mat are 

representative of average wastewater 

generation rates. 

§63.145 Process wastewater provision*— 

test methods and procedures to determine 

compliance. 

~(a) This paragraph applies to the use 

of all performance tests to demonstrate 

compliance of a treatment process or 

waste management unit. 

(1) The test shall be conducted when 

the treatment process or waste 

management unit is operating dt a 

representative inlet wastewater stream 

flow rate and VOHAP concentration 

under which it would be most difficult 

to demonstrate compliance. — -

(2) Operations during periods of 

startup, shutdown, or malfunction shall 

not constitute representative conditions' 

for the purpose ofa test 

(3) All testing equipment shall be 

prepared and installed as specified in 

the appropriate test methods. - •: 

(4) The owner or operator shall record 

all process information as is necessary 

to document operating conditions 

during the test 

(b) This paragraph applies to the use 

of performance tests to demonstrate 

compliance of a treatment process with 

the parts per million by weight 

wastewater stream concentration limits 

at the outlet of the treatment process. 

(1) The total VOHAP average 

concentration shall be measured for 

compliance with the concentration 

alternatives specified in 

§ 63.138(c)(l)(ii)(C) and (d)(l)(i) of this 

subpart; or the average concentration of 

each VOHAP shall be measured for 

compliance with the concentration 

alternatives specified in 

§ 63.138(b)(l)(ii)(A) of this subpart 

(2) A minimum of three representative 

samples of the wastewater stream 

exiting the treatment process shall be 

collected and analyzed using the 

procedures in § 63.144(b)(3) of this 

subpart. 

(c) This paragraph applies to the use 

of performance tests to demonstrate 

compliance of a noncombustion 

treatment process with the percent 

reduction limits for total VOHAP mass 

flow rate or VOHAP mass flow rote for 

strippability groups of HAP's. '•' -

(1) The percent reduction of total 

VOHAPmass flowrate shall be . 

measured for compliance with . 

§ 63.i38(c)(l)(ii)(B) or (c)(l)(iii)(B) of 

this subpart; or df VOHAP mass flow 

rate for strippability groups of HAP's for 

compliance with §63.138(b)(l)(ii)(C), 

(b)(l)(iii)(A). (c)(l)(ii)(D), or (c)(l)(tii)(Q 

of this subpart 

(2) The same test method shall be 

used to analyze the wastewater samples 

from both the inlet and outlet of the 

treatment process. . -..-•.. 

(3) The mass flow rate of total VOHAP 

or of VOHAP for a strippability group of 

HAP's entering the treatment process. 

(Eh) and exiting the treatment process 

(EJ shall be determined by computing 

the product of the flow rate of the 

wastewater stream entering or exiting 

the treatment process, arid the total 

VOHAP or strippabilitygroup VOHAP 

average concentration of the entering or 

exiting wastewater streams, 

respectively! ',•>"" 

(1) the flow rate of the entering and 

exiting wasteWater streams shall be 

detennined using the inlet and outlet 

flow meters, respectively. •..•;• 

(ii) The total VOHAP or strippability 

group VOHAP average concentrations of 

the entering and exiting wastewater 

streams shall be determined using the 

method specified in § 63.144(b)(3)(iii) of 

this subpaitl V 

(iii) Three grab samples ofthe -.-. • 

entering wastewater stream shall be 

taken at equally spaced time intervals 
P.20 

Federal Register / Vol. 58, N a 37 / Friday, February 26, 1993 / Corrections 

over a 1-hour period. Each 1-hour 

period constitutes a mn, arid the 

performance test shall consist of a 

minimum of 3 runs. 

(iv) Three grab samples of die exiting 

wastewater stream shall be taken at 

equally spaced time intervals ove? a Shour period. Eacb 1-hour period 

constitutes a run, and die perfonnance 

test shall consist of a minimum of 3 

runs conducted over the same 3-hour 

period at which the mess flow rate of 

total VOHAP or strippability group 

VOHAP entering the treatment process 

is determined. 

(v) The. mass flow rates of total 

VOHAP or strippability group VOHAP 

entering and exiting the treatment 

process are calculated as follows: 

K 

Eb = -

nxlO6 

(l^c.) 

K 

-(LVaAi ) 

nxlO6 

where: 

Eb=Mass flow rate of total VOHAP or 

strippability group VOHAP entering 

the treatment process, kilograms per 

hour. 

Ee=Mass flow rate of total VOHAP or 

strippability group VOHAP exiting 

the treatment process, kilograms per 

hour. 

K=Density of the wastewater stream, 

kilograms per cubic meter. 

Vbi=Average volumetric flow rate of 

wastewater entering the treatment 

process during esch ran i, cubic 

meters per hour. 

V^Average volumetric flow rate of 

wastewater exiting tbe treatment 

process during each run i, cubic 

meters psr hour. 

CM=Average concentration of total 

VOHAP cs- strippability group 

VOHAP in the wastewater stream 

entering the treatment process 

during each run i, parts per million 

by weight This shall be the sum of 

the average VOHAP concentrations 

of all HAP's in the stream, or of all 

HAP's in the target strippability 

group that are in the stream. 

Ccj=Average concentration of total 

VOHAP or strippability group 

VOHAP in the wastewater stream 

exiting the treatment process during 

each run i, parts per million by 

weisht This shaU be the sum of the 

average VOHAP concentrations of 

all HAP's In the stream or of all 

HAP's in the target strippability 

group that are in the stream. 

n=Number of runs. 

K 

(4) Tbe 

treatment 

follows: 

reduction across the. 

shall be calculated as 

R= K100 

where: 

R=Control efficiency of the treatment 

process, percent 

Eb=Mass flow rate of total VOHAP mstrippability group VOHAP entering 

ths treatment process, kilograms per 

hour. 

E„=Mass flow rate of total VOHAP or 

strippability group VOHAP exiting 

tbe treatment process, kilograms per 

hour. 

(d) This paragraph applies to die use 

ofa performance test to demonstrate 

compliance of a combustion treatment 7 

E

rocess with the percent reduction 

mite for total VOHAP mass flow rate 

or VOHAP mass flow rate for 

strippability groups of HAP's. Tbe 

percent reduction of total VOHAP mass 

flow rate shall be measured for 

compliance with §63.138{c)(lKiiKB) or 

(c)(l)(iii)(B) of this subpart; or of 

VOHAP mass flow rate for strippability 

groups of HAP's for compliance with 

§ 63.138|bKlMii)(a foHlHiiiXA), 

(c)(l)(iiMD). or (c)(l)(iiiHC) of this 

subpart 

(1) The mass flow rate of total VOHAP 

or of VOHAP for a strippability group of 

HAP's entering the combustion unit 

shall be detennined by computing tbe 

product of the average flow rate ofthe 

wastewater stream entering the 

combustion unit as determined by tb© 

inlet flow mete?, and tbe total VOHAP 

or group VOHAP average concentration 

of the waste stream, as determined using 

the sampling procedures in 

§ 63.144(b)(3) of this subpart. 

(2) Each 1-hour period constitutes a 

run, and the performance test shall 

consist of a minimum of 3 runs 

conducted over at least a 3-hour period. 

(3) If grab sampling techniques are 

used, then these grab samples shall be 

taken at a minimum of three equally 

spaced time intervals during the run. 

(4) Tbe mass flow rate of total VOHAP 

or strippability group VOHAP into the . 

combustion unit is calculated as 

follows: 

Eb = -

nxlO6 (5,w

) 

where: 

Eb=Mass flow sate of total VOHAP or 

strippability group VOHAP into tbe 

combustion unit kilograms per 

hour. 

K=Density of the waste stream, 

kilograms per cubic meter. 

V<=Average volumetric flow rate of 

waste entering the combustion unit 

during eacb run i, cubic meters per 

hour. 

Q=Average concentration of total 

VOHAP or strippability group 

VOHAP in the waste stream 

entering the combustion unit during 

each ?un i,parts-per million by 

weight. This "shaft ba the sum of the 

average VOHAP concentrations of 

all HAP's in the stream, or of all 

HAP's in the target strippability 

group that are in the stream. 

n=Number of runs. 

(5) The mass flow rate of total VOHAP 

or strippability group VOHAP exiting 

the combustion unit exhaust stack shall 

be determined BSMIOWB: 

(i) The time period for. the test shall 

not be less than '3 hours during which 

at least three 1-hour runs are conducted 

and ba the same time period at which 

the mass flow rate of VOHAP entering 

the treatment process is determined. 

Eacfe run shall represent a timeintegrated composite sample 

corresponding to tbe periods when the 

waste feed is sampled. 

(ii) A run shall consist of a 1-hour 

period during the test For each run: 

(A) The volume exhausted shall be 

determined using Method 2,2A, 2C, pr 

2D from appendix A of 40 CFR part 60, 

as appropriate. '.••-•-

(B) Tbe total VOHAP or strippability 

group VOHAP average concentration in 

the exhaust downstream of tbs 

combustion unit shall bs determined 

using Method is of appendix A of 40 

CFR part SO. Alternatively, any other 

test method validated according to the 

procedures in Method 301 of appendix 

A of this part 

(iii) The mass of total VOHAP qr 

strippability group VOHAP emitted 

duririg each run shall be calculated as 

follows: 

Mi = — I 0.0416 MWjQ 

1 0 6j= l 

IMjaUMii lAi 
P.21 

11686 Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

where: 

Mi=Mass of total VOHAP or 

strippability group VOHAP emitted 

during run i, kilograms. 

V=Volume of air-vapor mixture 

exhausted at standard conditions, 

cubic meters. 

6Q=VOHAP concentration of 

compound j measured in theexhaust, 

parts per million by volume. 

MWj=Molecular weight of compound j 

in exhaust stream, kilograms per 

kilogram-mole. 

m=NumDer of HAP compounds in total 

or in strippability group. 

0.0416=Conversion factor for molar 

volume, kilogram-mole per cubic 

meter at 293 "Kelvin and 760 

millimeters mercury absolute. . 

(iv) The total VOHAP or strippability 

group.VOHAP mass emission rate in the 

exhaust shall be calculated as follows: 

(|M,)/T 

where: 

Ea=Mass flowrate of total or 

strippability group VOHAP emitted, 

kilograms per hour.. -

Mj=Mass of total or strippability group 

VOHAP emitted during run i, 

. kilograms. . 

T=Total time.of-all runs, hours. 

n=Number of runs. 

(6) The total VOHAP or strippability 

group VOHAP destruction efficiency for 

the combustion unit shall be calculated 

as follows: 

Eb—Eo 

R= — X100 

E„' 

where: 

R = Total or strippability group VOHAP 

destruction efficiency for the 

combustion unit, percent. 

Eb = Mass flow rate of total or 

strippability group VOHAP entering 

the combustion unit, kilograms per 

hour. 

E0 = Mass flow rate of total or 

strippability group VOHAP exiting 

the combustion unit, kilograms per 

hour. 

(e) An owner or operator shall test 

equipment for emissions of 500 parts 

per million by volume or greater 

required in §§63.133 through 63:137 

and 63.139 of this subpart in accordance 

with the following requirements: 

(1) Monitoring shall comply with 

Method 21 from Appendix A of 40 CFR 

part 60. 

(2) The detection instrument shall 

meet the performance criteria of Method 

21. 

(3) The instrument shall be calibrated 

before use on each day of its use by the 

procedures specified in Method 21. 

(4) Calibration gases shall be: 

(i) Zero air (less than 10 parts per 

million by volume of hydrocarbon in 

air); and 

(ii) A mixture of methane and air at 

a concentration of approximately, but 

less than, 500 parts per million by 

volume methane. 

(iii) The instrument may be calibrated 

at a higher methane concentration up to 

2,000 parts per million by volume 

higher than the leak definition 

concentration for a specific piece of 

equipment for monitoring that piece of 

equipment. The instrument may not be 

calibrated at a methane concentration 

lower than the leak definition 

concentration for a specific piece of 

equipment. • :-\ 

(5) The background level shall be 

determined as set forth iri Method 21. 

(6) The instrument probe shall be 

traversed around all potential leak 

interfaces as close as possible to the 

interface as described in Method 21. 

(7) The instrument response factors 

shall be considered according to 

paragraphs (e)(7)(i) and (e)(7)(ii) of this 

section. 

(i) The response factors used shall be 

the instrument response factor 

detennined for the predominant HAP 

(i.e., the HAP present at the highest 

percentage) at 500 parts per million by 

volume. The response factors may be 

obtained from the available literature, 

the instrument manufacturer, or 

detennined for the specific instrument 

and HAP. 

(ii) Chemical composition of 

individual process streams may be 

determined by sampling, engineering 

calculations, or process knowledge. A 

separate detennination for each stream 

is not necessary if all or portions of the 

process unit can be shown to exhibit 

similar composition. The basis for all 

process stream composition 

determinations shall be. documented as 

required in § 63.144(b) of this subpart. 

(8) The arithmetic difference between 

the maximum concentration indicated 

by the instrument and the background 

level is compared to 500 parts per 

million by volume for determining 

compliance. 

(f) A performance test to demonstrate 

compliance of a vent stream control 

device with the organic compound 

reduction efficiency requirement 

specified under § 63.139(b) of this 

subpart shall use the following 

procedures: 

(1) Sampling sites shall be selected 

using Method 1 or IA from appendix A 

of 40 CFR part 60, as appropriate. 

(2) The mass flow rate of organics 

entering and exiting the control device 

shall be determined as follows: 

(i) The time period for the test shall 

not be less than 3 hours during which 

at least three runs are conducted. 

(ii) A run shall consist of a 1-hour 

period during the test. For each run: 

(A) The volume exhausted shall be 

determined using Method 2, 2A, 2C, or 

2D from appendix A of 40 CFR part 60, 

as appropriate; 

(B) The organic concentration in the 

vent stream entering and exiting the 

control device shall be determined 

using Method 18 from appendix A of 40 

CFR part 60. Alternatively, any other 

test method validated according to the 

procedures in Method 301 of appendix 

A of this part may be used. 

(iii) The mass flow rate of organics 

entering and exiting the control device 

during each run shall be calculated as 

follows: 
Federal Register / Vol. 58, No. 37 /Friday, February 26, 1993 /Corrections 11687 

0.0416 -

K3 = —- U Vaj ICai^MW, 

106xm

 lj=1

- \l =1 / J 

0.0416 f m .„ 

Eb = [ L_yhi (^CwjMWi) J 

106x m 

where: 

E.=Mass flow rate of organics exiting the control; device, kilograms per hour. 

Eb=Mass flow rate of organics entering the control device, kilograms per hour. 

V^=Average volumetric flow rate of vent stream exiting the control device during run j at standards conditions, cubic 

meters per hour. 

Vbj=Average volumetric flow rate of vent stream entering the control device during run j at standards conditions, cubic 

meters per hour. 

m=Number of runs. 

Cuij=Organic concentratibn of .compound i measured in the vent stream exiting the control device during run j as 

determined by Method 18. parts per million by vbluirie On a dry basis. 

Chij=Organic concentration of compound i measured in the vent stream entering the control device during run j as 

determined by Method 18, parts per million by volume on a dry basis. 

MVVi=Molecular weight of organic compound i in the vent stream, kilograms per kilogram-mole. 

n=Number of organic compounds in the vent stream. 

0.0416=Conversion factor for molar volume, kilograms-mole per cubic meter'at 293 "Kelvin and 760 millimeters mercury 

absolute. 

(4) The organic reduction efficiency 

for the control device shall be calculated 

es follows: 

E„-E. 

R= X100 

Eb 

where: 

R=Total organic reduction efficiency for 

the control device, percent 

Eb=Mass flow rate of organics entering 

the control device, kilograms per 

hour. 

Ea=Mass flow rate of organics exiting the 

control device, kilograms per hour. 

(g) A perfonnance test to demonstrate 

compliance with the mass removal 

provision for new SOCMI process units 

in §63.138(b)(l)(iii)(C) of this subpart 

shall consist ofa determination of mass 

removal required to be achieved, and a 

detennination of mass removal actually 

achieved. Actual mass removal and 

compliance shall be determined by the 

procedure in paragraph (i) of this 

section. The required mass removal for 

each Group 1 wastewater stream prior to 

combination of the streams for treatment 

shall be detennined using the following 

equation: 

RMR K 

I O 6 

n V E 

3 = 1 

0.9 9 

where: 

RMR=Required mass removal of 

VOHAP from Table 8 HAP 

compounds in a Group 1 

wastewater stream, in kilograms per 

year. 

KcDensity of the Group 1 wastewater 

stream, kilograms per cubic meter. 

V=Annual wastewater quantity ofthe 

Group 1 wastewater stream, cubic 

meters per year. 

n=Number of Table 8 HAP compounds 

in stream. 

£j=Average VOHAP concentration of 

eacb Table 8 organic HAP 

compound "j " in the Group 1 

wastewater stream at the point of 

generation, parts per million by 

weight 

0.99sRequired removal fraction of 

VOHAP from Table 8 Compounds. 

(1) The annual wastewater quantity 

fbr each Group 1 wastewater stream to 

be combined for treatment (V), shall be 

determined using the procedures 

specified in paragraph (a) of this 

section. 

(2) The VOHAP average concentration 

of each Table 8 HAP compound (Cj) in 

each Group 1 wastewater stream to be 

combined for treatment shall be 

determined using the procedures 

specified in § 63.144(b)(3) of this 

subpart. 

(3) The total required mass removal is 

calculated by adding together the 

required mass removal for each" 

individual Group 1 stream to be 

combined for treatment 

(h) A performance test to demonstrate 

compliance with the mass removal 

provisions for new and existing SOCMI 

process units in § 63.138(c)(l)(iii)(D) of 

this subpart shall consist of a 

determination of mass removal required 

to be achieved, and a determination Of 

mass removal actually achieved. Actual 

mass removal and compliance shall be 

determined by the procedure in 

paragraph (i) of this section. The 

required mass removal for each Group 1 

wastewater stream prior to combination 

of the streams for treatment shall be 

determined using the following 

equation: 
P.23 

11688 Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

RMR -T^ v

^

1 h •••! 00 

where: * 

RMR=Required mass removal of total 

VOHAP average concentration in 

the Group 1 wastewater stream, 

prior to combination with other 

Group 1 wastewater streams, 

kilograms per year. 

K=Density of the Group 1 wastewater 

stream, kilograms per cubic meter. 

V=Average wastewater flow rate for the 

Group 1 wastewater stream, cubic 

meters per year. 

n=Number of organic HAP compounds 

in stream. 

CJ=Average VOHAP concentration of 

compound "j" in the Group 1 

wastewater stream at the point of 

generation, parts per million by 

weight. 

F=Required percent removal, of each 

compound "j" (target removal 

'*» : efficiency from Table 9). 

(1) The average wastewater flow rate 

for each Group 1 wastewater stream to 

be combined for treatment (V), shall be 

determined using the procedures 

specified in § 63.144(e) of this subpart. 

(2) The average of each VOHAP 

concentration (Cj) in each Group 1 

wastewater stream to be combined for 

treatment shall be determined using the 

procedures specified in § 63.144(b)(3) of 

this subpart. 

(3) The total required mass removal is 

calculated by adding together the 

required mass removal for each . •: . . 

individual Group 1 wastewater stream 

to be combined for treatment. 

(i) For a performance test to 

demonstrate compliance of a treatment 

process with the mass removal . 

standards, the actual mass removal of 

total VOHAP (for compliance with, 

§63.138(c)(l)(iii)(D) of this subpart) or 

of VOHAP from table 8 compounds (for 

complianco with §63.138(b)(l)(iii)(C) of 

this subpart] in the wastewater stream 

shall be determined by the following 

procedure: 

(1) The actual mass removal of a 

treatment process, or series of treatment 

E

rocesses other than a properly operated 

iological treatment unit shall be 

determined using the following 

equation: 

MR^b-EJ 

where: ' . 

MR=Actual mass removal by the 

treatment process or series of 

treatment processes of total VOHAP 

for Table 9 HAP compounds or 

VOHAP from Table 8 HAP 

compounds, kilograms per hour. 

Eb=Mass flow rate of total VOHAP for 

Table 9 HAP compounds or VOHAP 

from Table 8 HAP compounds 

entering the treatment process or 

series of treatment processes, 

kilograms per hour. 

En=Mass flow rate of total VOHAP for 

Table 9 HAP compounds or VOHAP 

from Table 8 HAP compounds 

exiting the treatment process or 

series of treatment processes, 

kilograms per hour. 

(i) The mass flow rate of total VOHAP 

for Table 9 HAP compounds or VOHAP 

from Table 8 HAP compounds entering 

the treatment process (Eb) shall be 

determined using the procedures 

specified in paragraph (c)(3) of this 

section. 

(ii) The mass flow rate of total 

VOHAP for Table 9 HAP compounds or 

VOHAP from Table 8 HAP compounds 

exiting the treatment process (EJ shall 

be determined using the procedures 

specified in paragraph (c)(3) of this 

section.' 

(2) The actual mass removal (MR) of 

a treatment process which is a properly 

operated biological treatment unit is ' 

equal to the mass removed due to 

biological destruction. The mass 

removal mould be determined using the 

following equation: 

MR=(Eb-E«)*Fbio 

where: 

MR=Actual mass removal by the 

treatment process or series of 

treatment processes of total VOHAP 

for Table 9 HAP compounds or 

VOHAP from Table 8 HAP 

compounds, kilograms per hour. 

Eb=Mass flow rate of total VOHAP for 

Table 9 HAP coiripounds or VOHAP 

from Table 8 HAP compounds 

entering the treatment process or 

series of treatment processes, 

kilograms per hour. . 

Ea=Mass flow rate of total VOHAP for 

Table 9 HAP compounds or VOHAP 

from Table 8 HAP compounds 

exiting the treatment process or 

series of treatment processes, 

kilograms per hour. 

Fbi„=The fraction of VOHAP from Table 

8 HAP compounds, or total VOHAP 

for Table 9 HAP compounds,, 

biodegraded in a properly operated 

biological treatment unit. This 

fraction shall be determined using 

WATER7. The site specific biorate 

constants used as inputs to 

WATER7 shall be deterrriined using 

Method 304 of appendix A of this 

part. ' 

(3) Compliance with the riiass removal 

provisions in §63.138(b)(l)(iii)(C) or 

§63.138(c)(l)(iii)(D) of this subpart is 

achieved when the actual mass removal 

of tbe treatment process (MR) is 

demonstrated to meet or exceed the total 

required mass removal (RMR), 

determined using the procedures 

specified in paragraphs (g) or (h) of this 

section, respectively. 

§63.150 . Emlaolono averaging provlolons. 

(a) This section applies to owners or 

operators who seek to comply with 

emission limits by using emissions 

averaging according to § 62.112(c)(2) of 

this subpart rather than following the 

provisions of §§ 63.113 through 63.149 

of this subpart for all emission points. 

(b) Unless an operating permit, 

application has been submitted, the 

owner or operator shall develop, and 

submit for approval, an Implementation 

Plan containing all bf the information 

required in § 63.151(d) of this subpart 

for all points to be included in an 

emission average. The Implementation 

Plan or operating permit application 

shall identify all emission points to be 

included in the emissions averaging. 

This must include any Group 1 ' 

emission points to which the reference 

control technology (defined in § 63.111 

of this subpart) is not applied and all 

other emission points being controlled 

as part ofthe average. -

(c) The following emission points can 

be credited in an emissions average to' 

offset use of controls less stringent than 

the reference technology on Group 1 

emission points, if sufficient 

information is available to determine

 : 

the appropriate value of credits for the 

point: 

(1) A Group 2 emission point-to 

which a new control has been applied 

after November 15,1990. 

(2) A Group 1 emission point that is * 

controlled by a technology that the 

Director of the EPA Office of Air Quality 

Planning and Standards or the operating 

permit authority agrees has a higher 

nominal control efficiency than the . 

reference technology if the emission 

point Was not controlled to this level on 

or before November 15,1990.' •; 

Information on the nominal control 

efficiencies for such technologies must 

be submitted and approved as provided 

in paragraph (h) of this section. -

;

 • 

(3) Emission points from which : 

emissions are reduced hy pollution , . 

prevention projects initiated: after 1987. 

For Group, 1 emission points, in order tb 

be credited, the pollution prevention 

1

>rojects must result in emission levels , 

ower than what would have occurred if 

the reference technology had been 

applied to the emission points at their 

emission levels prior to pollution 
prevention. Pollution prevention is 

defined in paragraph (i) of this section. 

(4) Any Group 2 emission point to 

which controls were applied as part of 

the early reduction program established 

by the EPA under section 112(i)(5) of 

the Clean Air Act as amended in 1990 

(56 FR 27338). 

(5) A Group 1 emission point 

controlled by a technology EPA agrees 

has a higher nominal control efficiency 

than the reference technology if this 

control was applied as part of the early 

reduction program established by the 

EPA under section 112(i)(5) of the Clean 

Air Act as amended in 1990 (56 FR 

27338). 

(6) Any Group 2 emissions point to 

which controls were applied as part of 

a commitment under the Agency's 33/50 

program described in EPA Publication 

Number EPA-741-K-92-OQ1. 

(7) Any Group 1 emissions point 

controlled by a technology EPA'agrees 

has a higher nominal control efficiency 

than the reference control technology if 

the control was applied as part of a 

commitment under the Agency's 33/50 

program described in EPA Publication 

Number BPA-741-K-92-i0pi. 

(d)The following emission points 

cannot be iised to generate credits in 

emission averaging: . > 

(1) Emission points already controlled 

on or before November 15,1990, except 

those that were controlled as part ofthe 

Section 112(i)(5) early reduction 

program, the 33/50 prograrii, or a 

pollution prevention program aS 

described in paragraph (c) of this 

section. • y 

(2) Emission points achieving control 

levels higher than; the nominal 

efficiency of a reference technology 

when using a reference control 

technology, unless the requirements of 

§ 63.150(h)(6) of this subpart have been 

satisfied for process vents, or the 

requirerrierits in §63.S50(g)(3)(ii)(C) or 

(g)(3)(iii)(D) have been satisfied for 

storage vessels. For example, if is not 

allowable to claim that an internal 

Abating roof meeting the specifications" 

of § 63.119(b) of this Subpart applied to 

a storage vessel is achieving greater than 

95 percent control. '. ' . , 

. (3) Production cutbacks and 

shutdowns. The .emission credits are 

calculated at the actual monthly 

production level and do not include any 

process units that are shut down, 

(e) For all points included >n an 

emission average, the owner or operator 

shall:-' - :'•:-• = •••: ••:•>-••• • > "' ; : 

(1) Calculate and record monthly 

debits for all Group 1 emission points 

that are controlled to a level less 

stringent than the reference technology 

level for those emission points. 

Equations in paragraph (f) of this section 

shall be used to calculate debits. 

(2) Calculate and record monthly 

credits fbr all Group 1 or Group 2 

emission points that are overcontrolled 

to compensate for the debits using 

equations in paragraph (g) of this 

section. Emission points that meet the 

criteria of paragraph (c) of this section 

may be included in the credit 

calculation, whereas those described in 

paragraph (d) of this section shall not be 

included. ..'.';. 

(3) Demonstrate that annual credits 

calculated according to paragraph (g) of 

this sectiori are greater than or equal to 

debits calculated for the same annual 

compliance period according to 

paragraph (f) of this section. If the 

credits are not greater than or equal to 

the debits for the same annua) 

compliarice period, and the owner or 

operator has met the requirements ih 

paragraphs (e)(3)(i) through (e)(3)(iv) of 

this section, the owner or operator may 

use banked credits arid credits from the 

relevant compliance period to offset the 

debits. If banked credits are available 

and necessary, compliance shall be 

judged based on the sum of banked 

credits and credits from the relevant 

compliance period, averaged with debits 

from the relevant compliance period. 

(i) If the credits 'calculated according 

to paragraph (g) of this section are 

greater than the debits calculated for the 

same annual compliance period 

according to paragraph (f) of this 

section, the owner or operator may bank 

the extra credits for use in future 

compliarice periods. 

(A) In Order to bank credits for use in 

future compliance periods, the owner or 

operator must report the data used fo 

calculate that the extra credits were 

generated and certify the accuracy of 

that data in the Periodic Reports as 

specified in § 63.152(c) of this Subpart. 

These records must be readily accessible 

for 5 years after the period iri Which the 

credit is available for use as specified iri 

paragraph (e)(3)(iy) of this section.,. 

(B) The owner or operator may choose 

to include more than, the required 

number of credit generating emission 

points in an average in order to increase 

the likelihood of creating bankable 

credits. However, these additional 

points are not required to create ... 

bankable credits. 

(ii) Banked credits can only be used 

tc comply with the annual requirement 

specified in paragraph (e)(3) of this 

section. Banked credits cannot be used 

for the quarterly requirement specified 

in paragraph (e)(4) of this section. 

(iii) In the Implementation Plan for 

emissions averaging as specified in 

§ 63.151(c) and (d) of tbis subpart or the 

operating permit application as 

specified in § 63.152(e) of this subpart, 

the credit generating emission points 

must be capable of generating sufficient 

credits to offset the debits from the debit 

generating emission points under 

representative operating conditions. The 

owner or operator shall not develop an 

Implementation Plan or operating 

permit application for emissions 

averaging that relies on banked credits 

to ensure that credits will exceed debits. 

If such ian averaging plan is submitted, 

it will not be approved. . , 

(iv) The length of time that banked 

credits shall be available for use after 

the year in which the extra credit was 

generated is (a range of 2 to 5 years is 

being proposed; a single number will be 

selected at promulgation). If a banked 

credit is hot used within (2 tb 5) years 

ofthe year in which if was generated, 

it is no longer available for use. 

(4) Demonstrate that debits calculated 

for a quarterly (3-month) period 

according to paragraph (f) of this section 

are not more than (a range of 1.25 to 

1.35 is being proposed; a single number 

willbe selected at promulgation) times 

the credits for the same period 

calculated according to paragraph (g) of 

this section. Compliance for the quarter 

shall be determined based on the ratio 

of credits and debits from that quarter, 

ivith (25 to 35) percent more debits than 

credits allowed on a quarterly basis. 

(5) Calculation of monthly credits and 

debits shall not include periods of 

startup, shutdown, and malfunction as 

described in the source's startup, 

shutdown, and malfunction plan 

required by § 63.6(e)(3) of subpart A of 

this part.16'. 

(6) The.quarterly and annual credits 

and debits shall be recorded and 

reported in the Periodic Reports as 

specified in § 63.152(c) of this subpart. 

The Periodic Reports shall include a 

certification of compliance with the 

emissions averaging provisions. 

(f) Debits shall ba calculated as 

follows: 

(1) The overall equation for : , 

calculating source-wide debits is: 

"The EPA Kill propose subpart A in the future. 

I — " —-
P.25 

11690 Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

Debits = I (EPViAc-, UAI.- (0:02 )EPV1 U )+.!.(ES.ACIIMI. - (0.05)ESiu) 

+ I-(CTRiACTUAL-(0.02)ETRlu) + 1 (E\VW IAC TVAI.-EWW 1 C ) 

I=I. •' I= I 

where; 

Debits and all terms of the equation are 

in units of megagrams per month, 

and 

EPViAcruAL=Emission8 from each Group 

1 process vent (i) that is not 

controlled to the level of the 

reference technology. This is 

calculated according to paragraph , 

(f)(2) of this section. . -

: 

(0.02) EPVu,=Emissions from each. 

Group 1 vent (i) if the reference 

control technology had been, 

applied to the uncontrolled 

emissions, calculated according to 

paragraph (f)(2) of this section. 

ESiAcruAL=Emissions from each Group 

' 1 storage vessel (i) that is not 

controlled to the level of the 

reference technology. This is 

calculated according tb paragraph 

(f)(3) of this section. 

(0.05) EStu=Emissions from each Group 

1 storage vessel (i) if the reference 

control technology had been 

applied to tbe uncontrolled 

emissions, calculated according to 

paragraph (f)(3) of this section. 

ETRiAcruAL=Emissions from each Group 

1 transfer rack (i) that is not 

controlled to the level of the 

reference technology. This is 

calculated according to paragraph 

(f)(4) of this section. 

(0.02) ETRja=Emissions from each 

:

" Group 1 transfer rack (i) if the 

;. reference control technology had. 

been applied to the uncontrolled 

emissions, calculated according to 

paragraph (f)(4) of this section. 

EWW(AcruAi.=Emissions from each 

Group 1 wastewater stream (i) that 

is not controlled to the level of the 

reference technology. This is 

calculated according to paragraph 

(f)(5) of this sectiori. 

EWWic~Emissions from each Group 1 

wastewater stream (i) if the 

reference control technology had 

been applied to the uncontrolled 

emissions. This is calculated 

according to paragraph (f)(5) of this 

section. 

n=The number of emission points being 

included in the emissions average. 

The value of n is not necessarily the 

same for process vents, storage 

vessels, transfer racks, and 

wastewater. 

(2) Emissions from process vents shall 

be calculated as follows: 

(i) For purposes of determining . 

process vent stream flow rate, organic 

HAP concentrations, and temperature, 

the sampling site shall be after the final 

product recovery device, if any recovery 

devices are present, before any 

combustion device, and before 

discharge to the atmosphere. Method 1 

or 1A shall be used for selection of the 

sampling site. 

(ii) The following equation shall be 

used for each process vent (i) to 

calculate EPVh,: 

EPV1U = -

"(7.31xlO-'')Qh(LCJMJ') 

vJ=i ; 

T •+ 273 

where: 

EPVia=Uncontrolied process vent 

emission rate from process vent (ij 

in megagrams per month. 

Q=Vent stream flow rate (dry standard 

cubic meters per minute) measured 

using Method 2,2A, 2C, or 2D of 

part 60, appendix A, as appropriate. 

h=Monthly hours of operation during 

which positive flow is present in 

the vent 

Cj=Concentration (parts per million by 

volume, dry basis) of organic HAP 

compound j as measured by Method 

18. 

Mj=Molecular weight of organic HAP 

compound j (gram/gram-mole). 

T=Vent stream discharge temperature, 

in°C. ... 

n=Number of organic HAP compounds; 

(A) TTie values of OjQ,Mj, and f ^ ' 

shall be determined during' an initial 

performance test conducted under 

representative operating conditions. 

Monthly testing is not required. 

(B) If there is a change in capacity 

utilization other than a change in . 

monthly operating hours; or if any other 

change is made to the process or 

product recovery equipment or 

operation such that the previously 

measured values of Q, Q, Mj, or Tare . 

no longer representative, a new 

perfonnance test shall be coriduc 

(iii) the following procedures and 

equations shall be used to calculate 

EPVIACTUAL: 
P.26 

(A) If the vent is not controlled by a 

control device or pollution prevention 

measure EPVtAcruAL=EPVto, where 

EPVh, is calculated according to the 

procedures in paragraphs (f)(2)(i) and 

(f)(2)(ii) of this section, 

(B) If the vent is controlled using a 

control device or a pollution prevention 

measure achieving less than the 98-

percent reduction level associated with 

the reference control technology, 

EPViAcruAL=EPViux 

U) Percent reduction shall be initially 

measured according to the procedures 

in §63.116 of this subpart if a 

combustion device is used. If a noncombustion control device is used, 

percent reduction shall ba demonstrated 

by an initial performance test at the 

inlet and outlet ofthe control device or. 

if testing is not feasible, by a control 

design evaluation arid documented 

engineering calculations. 

[2) For process vents, product 

recovery devices shall not be considered 

control devices and cannot be assigned 

a percent reduction in calculating 

EPViAcruAL. The sampling site for 

measurement of uncontrolled emissions 

is after the final product recovery 

device. However, as provided in 

§ 63.113(a)(3) of this subpart, a Group 1 

process vent may add sufficient product 

( * . 

Percent reduction 

100% ) 

recovery to raise the TRE index value 

above 1.0, thereby becoming a Group 2 

process vent 

(3) Procedures for calculating the 

percent reduction of pollution 

prevention measures are specified in 

paragraph (i) of this section. 

(3) Emissions from storage vessels 

shall be calculated as follows: 

(i) The following equation shall be 

used for each storage vessel (i) to 

calculate ESh,: 

C-biU 

LB + Lw 

12 

ESlu=Uncontrolled emissions from a 

fixed roof vessel having identical 

dimensions and vessel color as 

vessel i, in megagrams per month. 

Ln=Breathing loss emissions in 

megagrams per year calculated 

according to paragraph (f)(3)(i)(A) of 

this section. 

Lw=Worklng loss emissions in 

megagrams per year calculated 

according to paragraph (f)(3)(i)(B) of 

this section. 

(A) Breathing loss emissions shall be 

calculated using the following equation: 

where: 

L B 1.0 2 x 10 _!>M, 

where: 

Lti=Breathing loss emissions 

(megagrams per year). 

Mv=Molecular weight of vapor in 

storage vessel (pound/pound mole). 

PA=Average atmospneric pressure 

(pounds per square inch absolute). 

P=True vapor pressure of the HAP at 

liquid storage temperature (pounds 

per square inch absolute). See Table 

20 of this subpart. 

D=Tank diameter (feet). 

H=Average vapor space height (feet). 

Use vessel-specific values or an 

assumed value of one-half the 

height 

AT=Average ambient diurnal 

temperature change (°F). A typical 

value of 20 °F may be used. 

Fp=Paint factor (dimensionless) from 

Table 21. 

(^Adjustment factor for small diameter 

tanks1 (dimensionless); use C=l for 

diameter 230 feet; use 

C=0.0771D-0.0013D?-0.1334 for 

diameter <30 feet. 

- P )°-

6 8 D 1 7 3 H 0.51 A T 0.50 F p C K c 

Kc=Product factor (dimensionless). Use 

1.0 for volatile organic HAP's. 

(B) Working losses shall be calculated 

using the following equation: 

Lw=1.089xl0-8 MV(P) (V) (N) (KN) (KC) 

where: 

V=Tank capacity (gallon). 

N=Number of turnovers per year. 

KN=Turnover factor (dimensionless). 

180+N 

KN= for turnovers >36 

6N 

KM=1 for turnovers £36. ' 

M„ P, and Kc as defined in paragraph 

(A) above. 

(ii) The following equations shall be 

used for each fixed roof storage vessel 

(i) to calculate in ESJACTUAL. in ....,, 

megagrams per month: 

(A) If the vessel is not controlled with 

an intemai floating roof, an external 

floating roof, a closed vent systom and 

control device, or another control 

technique, ESiAcruAL=ESfa, where ESto is 

calculated according to the procedures 

in paragraph (f)(3)(i) of this section. 

(B) If the vessel is controlled using a 

control device or pollution prevention 

measure achieving less than the 95 

percent reduction level associated with 

the reference control technology, 

ESiAcnj, AO-ES*) 

1-Percent reduction 

100 

(C) If the vessel is controlled with an 

intemai or external floating roof that 

doss net meet the specifications of 

§ 83.1 S9 (b), (c), or (d) of this subpart, 

ESIACTOAL shall ba calculated as 

specified in paragraph (fK3Kiii) or 

(f)(3)(iv) of this section. 

(iii) Tiie foliowing equation shall be 

used for each internal floating roof 

vessel (i) that does not meet the 

BB 
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11692 Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

specifications of § 63.119(b) or (d) of 

this Subpart to calculate ESIACTTJAL in 

megagrams per month: 

ESiACTUALLW+LR+LP+LD 

12 

where: 

Lw=Withdrawal loss emissions in megagrams per year calculated according to paragraph (f)(3)(iii)(A) of this section. 

LR=Rim seal loss emissions in megagrams per year calculated according to paragraph (f)(3)(iii)(B) of this section. 

L,F=Fitting loss emissions in megagrams per year calculated according to paragraph (f)(3)(iii)(C) of this section. 

Lo=Deck seam loss emissions in megagrams per year calculated according to paragraph (f)(3)(iii)(D) of this section. 

(A) Withdrawal loss emissions shall be calculated using the following equation: 

L\v = -

1.018 xlO"5 QCWL 

D 

where: 

Q=Throughput (gallon per year); (gallon/turnover) * (turnovers per year). 

C=Shell clingage factor (barrel/1,000 feet2), see Table 22 of this Subpart. 

WL=Average liquid density (pound/gallon). 

D=Tank diameter (feet). 

N<~Number of columns (dimensionless), see Table 23 of this subpart. 

Fc=Effective column diameter (feet) (column perimeter (feet) 3.1416], see Table 24 of this subpart. 

(B) Rim seal loss emissions shall be calculated using the following equation: 

KSV"P xDMvK. 

L R = -

2204.6 

where: 

Mv=Molecular weight of vapor in 

storage vessel (pound/pound mole). 

PA=Average atmospheric pressure 

(pounds per square inch absolute). 

P=True vapor pressure at liquid storage 

temperature (pounds per square 

inch absolute). 

D=Tank diameter (feet). 

Kc=Product factor (dimensionless); use 

1.0 for organic HAP's. 

K,=Seal factor. [pound-mole/(feet (miles 

per hour)" year)], see Table 25 of 

this subpart. 

V=Average wind speed at the source 

(miles per hour). A value of 10 

miles per hour may be assumed if 

source-specific data are not 

available. 

n=Seal related wind speed exponent 

(dimensionless), see Table 25 of this 

subpart. 

P*=Vapor pressure function 

(dimensionless), 

(C) Fitting loss emissions shall be 

calculated using the following equation: 

P = 

_P_ 

PA 

M'-^H 

Fitting Loss (Mg/yr) =• 

FfP-xMvKc 

2205 

where 

Fr The total deck fitting loss factor 

(pound mole per year), and 

n 

Ff " . £ ("Fi K F i ) " !< N F!

 KFj.) * ( N F 2 Kp2 ) * • < % n * F n » 

where: 

Nn=Number of fittings of a particular type (dimensionless). NH is detennined for the specific tank or estimated from 

Tables 23 and 26 of this subpart. 

Kn=Deck fitting loss factor for a particular type fitting (pound mole per year). Kn is determined for each fitting type 

from Table 26 of this subpart. 

n=Number of different types of fittings (dimensionless). 

2205=Constant (pound/megagram). 

P°, Mv, Kc=as defined above. 

(D) Deck seam loss emissions shall be calculated using the following equation: 
P.28 

Federal Register / VoL 58. Na 37 / Friday, February 26, 1993 / Corrections 11693 

Deck Seam Loss (Mg/yr) =-

KDSDD2PXMVKC 

2204 6 

where: 

Kf>=Deck seam loss factor (pound-mole/feet year). 

=0.34 for non-welded decks. 

=0 for welded decks. 

So=Deck seam length factor (feet/feet2), see Table 27 of this subpart. 

D, P*, Mv, Kc=as defined above. 

(iv) The following equation shall be 

used for each external floating roof 

vessel (i) does not meet the 

specifications of § 63.119(c) of this 

Subpart to calculate ES^CTUAL in 

megagrams per month: 

ESiAc 

LW+LR+LP 

12 

where: 

Lw=Withdrawal loss emissions In 

megagrams per year calculated 

according to paragraph (f)(3)(iv)(A) 

of this section. 

Lp=Rim seal loss emissions in 

megagrams per year calculated 

according to paragraph (f)(3)(iv)(B) 

of this section. 

Lp=Fitting loss emissions in megagrams 

per year calculated according to 

paragraph (f)(3)(iv)(C) of this 

section. 

(A) Withdrawal loss emissions shall 

be calculated using the following 

equation: 

Lw=4.28*10-» QCWJD 

where: 

Q=Throughput (gallons per year). 

C=Shell clingage factor (barrel per 1,000 

feet2), see Table 22 of this subpart. 

Wi.=Average liquid density (pound/ 

gallon). 

D=Vessel diameter (feet). 

(B) Seal loss emissions shaii be 

calculated using the following equation; 

LSE=K,VNP*DM,KC/2205 

where: 

K,=Seal factor, see Table 28 of this 

subpart. 

V=Averago wind speed (miles per hour) 

at the source. A value of 10 miles 

per hour may be assumed if sourcespecific data are not available. 

N=Seal wind speed exponent, see Table 

28 of this subpart 

P*=Dimensionless vapor pressure 

function es defined in paragraph 

(f)(3)(iii)(B) of this section. 

D=Vessel diameter in feet. 

Mv=Molecular weight ofthe HAP fai 

pound/pou nd-mole. 

5Q=Dimensionless product factor (use 

1.0 for volatile organic HAP's). 

2205=Constant (pound/megagram). 

(C) Fitting loss emissions shall be 

calculated using the foliowing equation: 

LKP=FFP*M,KC/2205 

where: 

FF=The total deck fitting loss factor 

(pound mole per year). 

n 

- E <%!%!> = ((NF lKF l) + (Np2KF2) 

1 = 1 

( N F n K F n )] 

whore: 

Nn=Number of fittings of a particular type (dimensionless). NH is determined for the specific tank or estimated from 

Tables 29 through 31 of this subpart. 

KR=Deck fitting loss factor for a particular type fitting (pound mole per year). 

sKFaJ+Kpw V"5', see Table 29 of this subpart for the appropriate values of Kf», KRH and m for each fitting type. 

P*. Mv, K« = as defined above. 

(4) Emissions from transfer racks shall 

be calculated as follows: 

(i) The following equation shall be 

used for each transfer rack (i) to 

calculate ETRj„: 

ETRi^fl^OxlO-7) 

SPMG 

where: 

ETRte n Uncontrolled transfer emission 

rate, megagrams per month. 

S s Saturation factor (see Table 32 of 

this subpart). 

P » Weighted average rack vapor 

pressure of organic HAP's 

transferred at the rack during the 

month, kilopascals. 

M = Weighted average molecular weight 

of organic HAP's transferred at the 

rack during die month, gram/grammole. 

G s Monthly volume of organic HAP 

transfened, liters per month. 

T » Temperature of bulk liquid loaded. 

"Kelvin ("0273). 

(ii) The following equation shall be 

used for each transfer rack (i) to 

calculate the weighted average rack 

vapor pressure (P): 

J =n 

E <P3><Qj> 

where: 
11694 Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

P=Weighted average rack vapor pressure 

of organic HAP's transferred at the 

rack during the month, kilopascals. 

Pj=Vapor pressure of individual organic 

. HAP transferred at the rack, 

kilopascals. 

G=Monthly volume of organic HAP 

transferred, liters per month. 

Gj=Monthly volume of individual 

organic HAP transferred at the rack, 

liters. 

n=Number of organic HAP's transferred 

at the rack. 

(iii) The following equation shall be 

used for each transfer rack (i) to 

calculate the weighted average rack 

molecular weight (M): 

M = 

1 

where: 

M=Weighted average molecular weight 

of organic HAP transferred at the 

rack during a month, gram/grammole. 

Mj=Molecular weight of individual - • 

organic HAP transferred at the rack, 

gram/gram-mole. 

GpMonthty volume, of individual 

organic HAP transferred at the rack, 

liters per month. 

n=Number of organic HAP's transferred 

at the rack. 

(iv) The following procedures and 

equations shall be used to calculate 

ETRIACTUAL: 

(A) If the transfer rack is not 

controlled, ETRJACTUAL=ETRIU, where 

ETRm is calculated using the equations 

under paragraphs (f)(4)(i), (f)(4)(ii), and 

(f)(4)(iii) of this section. . 

(B) If the transfer rack is controlled 

using a control device or a pollution 

prevention measure achieving less tha» 

98 percent reduction level associated 

with the reference control technology 

level, 

ETRjACTUAi. - ETRj . . ( 

1 - Percent reduction 

100% ) 

(1) The percent reduction for a combustion or recovery device shall be initially measured according to the aquations 

and methods specified in § 63.128(a) of this Subpart. As other control techniques are used, percent reduction shall 

be demonstrated by an initial performance test or by a control design analysis and documented engineering calculations. 

(2) Procedures for calculating the percent reduction for pollution prevention measures are specified in paragraph 

(i) of this section. 

(5) Emissions from wastewater shall be calculated as follows: In paragraph (f)(5) of this section, the terms wastewater 

and wastewater stream are used to mean wastewater. 

(i) The following equation shall be used for each wastewater stream (i) to calculate EWWic: 

EWW1C = (6.0 xlO"8)Q,H, 1(1 - Frm)FemHAPim + (0.05)(6.0 x 10 i-K )Q,H, I (FrmHAPim) 

m=l 

where: 

EWWic=Monthly wastewater stream emission rate if wastewater stream (i) is controlled by the reference control technology, 

in megagrams per month. 

Qi=Average flow rate for wastewater stream (i), as detennined by the procedure in § 63.144(e)(3) of this subpart, in 

liters per minute. 

Hi=Number of hours during the month that wastewater stream (ij was discharged, in hours per month. 

Frro=Strippability factor of HAP compound (m) in wastewater, from Table 33 of tids subpart, dimensionless. 

Fem=Fraction emitted of HAP compound (m) in wastewater from Table 33 of this subpart, dimensionless. ,.. 

s=Total number of organic HAP compounds iri wastewater stream (i). 

HAPim=Average organic HAP concentration of compound (m) in wastewater stream (i), in parts per million by weight, 

as determined for the point of generation using the sampling procedure in §63.144(b)(3)(i) and (b)(3)(ii) of this 

subpart: To analyze the samples collected, (1) a test method or results from a test method that measures organic 

HAP concentrations in the wastewater, and that has been validated pursuant fo section. 5.1 or 5.3 of Method 

301 of appendix A of this Part may be used; or (2) the procedures in § 63.144(b)(3)(iii)(A) of this Subpart 

may be used to determine the term. Qm described below, and then HAPim may ba calculated from it using 

the following equation: HAPim=Ciro/Fmro, where Fmm for compound m is obtained from Table 13 of this Subpart. 

Cim=Average VOHAP concentration of HAP compoimd (m) in wastewater stream (i), as determined for the point of 

generation according to the procedures in § 63.144(b)(3) of this Subpart, in parts per million by weight 

(A) Values for Qj, Gm. and HAPim may ba determined during en initial perfonnance test conducted under representative 

conditions. The average value obtained from three test runs shall be used. Monthly testing is not required. 

(B) If there is a change to the process or operation such that the previously measured values pf Q, Cim, and 

HAPim are no longer representative, a new perfonnance test shall be conducted. 

(C) As an alternative fo the perfonnance testing specified in paragraphs (f)(5)(i) (A) and (B) of this section, Qj 

may be detennined from records or process knowledge as specified in § 63.144(a). and Qm and HAPh, may be determined 

through process knowledge as specified in § 63.144(b) of this Subpart. 
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.Federal Register I Vol. 58, Npf .37;: / jFriday, February 26, 1993 / Corrections 11695 

(ii) The following equation shall be used to calculate EWWIACTUAL for each wastewater stream (i) which is -nanaged 

in any wastewater tank, surface impoundment, container, individual drain system, or oil-water separator not meeting 

the requirements of §§63.133 through 63.137 of this Subpart, respectively, or any other waste management unit or 

treatment process not meeting the requirements of § 63.138(h) of this subpart: 

(6.0x10 

•'". m=l -

where: 

XEWWiAcruAL=Monthly wastewater stream emission rate if wastewater stream (i) is not controlled to 7 the level of the 

reference control technology, in megagrams per month, 

Oj, Hi, s, Fem, and HAPm are as defined and determined according to paragraph (f)(5)(i) of this section. 

(iii) The following equation shall be used to calculate EWWIACTUAL for each wastewater stream (i) for which all 

wastewater tanks, surface impoundments, containers, individual drain systems, and oil-water separators used to manage 

the wastewater stream meet the requirements of.§§63.133 through 63:137 of this subpart and any other waste management 

unit or treatment process, meets the requirements of §63.138(h) of this subpart, and wastewater stream (i) is not controlled 

to the level of the reference control technology: 

EWWiACTUAL= (6.0xlO-8)QiHi I [FemHAP^l -PRi m )l 

''.•.'. • m= l 

where: 

EWWiACTUAL=Morithly wastewater 

stream emission rate if wastewater 

stream (i) is not controlled to the 

level Of the reference control 

technology, in megagrams per 

month; 

PR4m=The efficiency of the treatment 

process, or series of treatment 

processes, which treat wastewater 

: stream (i), in reducing the emission 

potential of organic HAP compound 

(m) in wastewater, dimensionless, 

:

 as Calculated by: 

HAP;, HAP, 

"PRim —• 

im-out 

HAP, im-m 

where: ' .7' 

HAPin^brAyerage concentrationof HAP. compound (m), defined and detennined according to paragraph (f)(5)(i) of this 

section, in the wastewater entering the first treatment process in the series. 

HAPinw,w=Average concentration of HAP compound (iri), defined and determined according to paragraph (f)(5)(i) of this 

section, in the wastewater exiting me last treatment process in the series. 

R,=Organic reduction efficiency of the device used to control any vapor streams emitted and collected from wastewater 

stream (i) during treatirient,as deteririined according to the procedures in § 63.145(f) of this subpart. 

Qi; HI, s, Fem, and HAPiri, are as defined and determined according to paragraph (f)(5)(i) of this section. Values 

of CaAni. Gnww,, Gu,,, and HAPim may be measured during an, initial test or determined based on knowledge ais provided 

in paragraph (f)(5)(i)(A), (B), and (C) of this section. .; 

(g) Credits shall be calculated as follows: | . 

(1) The overall equation for calculating source-wide credits is: 
P.31 

11696 Federal Register /Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

Credits^ D I ((0.02)EPVllu-EPVliACTUAL) 

1=1 

i n 

+ D Z (EPV2JBASE- EPV2 iACTUAU i=l 

+ D I ((0.05)ESliu-ESliACTUAL) 

i = l 

+ D I (ES21BASE-ES2I ACTUAL) 

I=I 

+ D I ((0.02)ETR11U-ETRI .ACTUAL) 

1=1 

+ D I (ETR2,„ASE-ETR2IAC TUAL) 

i = l . 

+ D I ( EWW-1 ic - EW\V 1 iACTUAL ) 

i = l 

+ D E (EWW2iBASE-EWW2iAcTUAL) 

i = l 

where: 

Credits and all terms of the equation 

are in units of megagrams per month, 

and the baseline date is November 15, 

1990, except that for a pollution 

prevention measure initiated after 1987 

or a control applied as part ofthe early 

reduction program or the 33/50 

program, the baseline date is prior to 

initiation ofthe pollution prevention 

measure or the early reduction or 33/50 

program control strategy, and 

D=Discount factor=(A range of 0.8 to 1.0 

is proposed. A single number will 

be selected at promulgation). 

EPVliAcnjAL=Emissions for each Group 

1 process vent (i) that is controlled 

to a level more stringent than the 

reference control technology, 

calculated according to paragraph 

(g)(2) of this section. 

(0.02) EPVl|U=Emissions from each 

Group 1 process vent (i) if the 

reference control technology had 

been applied to the uncontrolled 

emissions. EPVliu is calculated 

according to paragraph (g)(2) of this 

section. 

EPV2iAcnjAL=Emissions from each 

Group 2 process vent (i) that is 

controlled, calculated according to 

paragraph (g)(2) of this section. 

EPV2IBASE=Emissions froiri each Group 

2 process vent (i) at the baseline 

date, as calculated in paragraph 

(g)(2) of this section. 

ESliACTUAL=Emissions froiri each Group 

1 storage vessel (i) that is controlled 

to a level more stringent than the 

reference control technology, 

calculated according to paragraph 

(g)(3) of this section. 

(0.05) ESI j„=Emissions from each Group 

1 storage vessel (i) if the reference 

control technology had been 

applied to the uncontrolled 

emissions. ESliu is calculated 

according to paragraph (g)(3) of this 

sectiori. 

ES2iAcruAL=Emissions from each Group 

2 storage vessel (i) that is 

controlled, calculated according to 

paragraph (g)(3) of this section. 

ES2iRASE=Emissions from each Group 2 

storage vessel (i) at the baseline 

date, as calculated in paragraph 

(g)(3) of this section. 

ETRliACTUAL=Emissions from each 

Group 1 transfer rack (i) that is 

controlled fo a level more stringent 

than the reference control 

technology, calculated according to 

paragraph (g)(4) of this section. 

(0.02) ETRliU=Emissions from each 

Group 1 transfer rack (i) if the 

reference control technology had . 

been applied to the uncontrolled 

emissions. ETRI iu is calculated 

according to paragraph (g)(4) of this 

section. 

ETR2iAcTUAL=Emissions from each 

Group 2 transfer rack (i) that are 

controlled, calculated according to 

paragraph (g)(4) of this section. 

ETR2iBASE=Emissions from each Group 

2 transfer rack (i) at the baseline 

date, as calculated in paragraph 

(g)(4) of this section. 

EWWliACTUAL=Emissions from each 

Group 1 wastewater stream (i) that 
P.32 

Federal Register /Vol . 58, No. 37 / Friday, February 26, 1993 /Corrections 11697 

is controlled to a level more 

stringent than the reference control 

technology, calculated according to 

paragraph (g)(5) of this section. 

EWWlit—Emissions from each Group 1 

wastewater stream (i) if the 

reference control technology had 

been applied to tbe uncontrolled 

emissions, calculated according to 

paragraph (g)(5) of this section. 

E\VW2iACTUAL=Emissions from each 

Group 2 wastewater stream (i) that 

is controlled, calculated according 

to paragraph (g)(5) of this section. 

EWW2iBASE=Emissions from each Group 

2 wastewater stream (i) at the 

baseUne date, calculated according 

to paragraph (g)(5) of this section. 

n=Number of Group 1 emission points 

included in the emissions average. 

The value of n is not necessarily the 

same for process vents, storage 

vessels, transfer racks, and 

wastewater; 

m=Number of Group 2 emission points 

included in the emissions average. 

The value of m is not necessarily 

the same for process vents, storage 

vessels, transfer racks, and 

wastewater. 

(2) Emissions from process vents shall 

be determined as follows: 

(i) Uncontrolled emissions from 

Group 1 process vents, EPVltu, shall be 

calculated according to tbe procedures 

and equations in paragraphs (f)(2)(i) and 

(f)(2)(h) of this section. 

(ii) The following procedures and 

equations: shall be used to calculate, 

actual emissions from Group 1 process 

vents, EPVliAcnjAL, 

(A) Ifa Group 1 process vent is 

controlled using a technology with an 

approved nominal efficiency greater 

than 98 percent or a pollution 

prevention measure achieving greater 

than 98 percent emission reduction. 

EPV1 .ACTUAL = EPVlj 

( ' -

Nominal efficiency % 

100% ) 

(B) The nominal efficiency shall be 

determined as described in paragraph 

(h) of this section for a control device 

and paragraph (i) of this section for a 

pollution prevention measure. 

(C) Combustion devices shall not be 

attributed a nominal efficiency greater 

than 98 percent, unless they have been 

assigned a higher nominal efficiency 

according to the procedures in 

paragraph (h) of this section. 

(iii) The following procedures shall be 

used to calculate actual emissions from 

Group 2 process vents, EPV2IACTUAL: 

(A) If a Group 2 process vent is 

controlled by a control device, a 

recovery device applied after 1987 as a 

pollution prevention project, or a 

pollution prevention measure achieving 

a percent reduction less than or equal to 

98 percent reduction level associated 

with the reference control technology, 

EPV2, ACTUAL -

EPV2mx 1 -

( 

Percent reduction 

100% ) 

(J) EPV2iu shall be calculated according to the equations and procedures in paragraph (f)(2)(i) arid (f)(2)(ii) of this 

section, except as provided in paragraph (g)(2)(iii)(A)(3) below. 

12) The percent reduction shall be calculated according to the procedures in paragraph (f)(2)(iii)(B)(J), (2), and (3) 

of this section, except as provided in paragraph (g)(2)(iii)(A)(4) below. . 

(3) If a recovery device was added as part of a pollution prevention project initiated after 1987, EPV2io shall be 

calculated prior to the recovery device... The equation in paragraph (f)(2)(ii) of this section shall be used to calculate 

EPV2i„; however, the sampling site for measurement of vent stream flow rate, organic HAP concentration, and temperature 

shall be at the inlet of the recovery device. 

(4) Ifa recovery device was added as part ofa pollution prevention project initiated after 1987, the percent reduction 

shall be demonstrated by conducting a performance test at the inlet and outlet of the recovery device. 

(B) If a Group 2 process vent is controlled using a technology with an approved nominal efficiency greater than 

98 percent or a pollution prevention measure achieving greater than 98 percent reduction, 

EPV2IACTUAL= EPV2; 0-

Nominal efficiency % 

•<"-•• 100 % ) 

(1) The nominal efficiency shall be detennined as described in paragraph (h) of this section for a control device 

or in paragraph (i) of this section for a pollution prevention measure. 
P.33 

11698 Federal Register /Vol . 58, No. 37 / Friday, February 26, 1993 /Corrections 

(2) Combustion devices shall not be attributed a nominal efficiency greater than 98 percent, unless they have been 

assigned a higher nominal efficiency according to the procedures in paragraph (h) of this section. 7 

(iv) Emissions from Group 2 process vents at baseline, EPV2iiBAsE, shall be calculated as follows: 

(A) If the process Vent was uncontrolled on November 15, 1990, EPV^BAiE = EPV2iu and shall be calculated according 

to the procedures and equations in paragraphs (f)(2)(i) and (f)(2)(H)i of this.section. 

(B) If the prbcess vent was controlled on November 15, 1990, and this control was not applied under either the 

33/50 or the early reduction program and was not the result of a pollution prevention measure. 

Percent reduction % 

EPV2iBASC = 

EPV2iu 

(

Percent reduction % v., 

; 100% :. ) 

Where EPV2i„ is calculated according to the equations in paragraphs (f)(2)(i) and (f)(2)(ii) of this section. The percent 

reduction shall be calculated according to the procedures specified in paragraphs (f)(2)(iii)(B) (1). (2). and.(3) of this 

section. 

(C) If a recovery device: was added to a process vent as part of a pollution prevention project initiated after 1987. 

EPV2IBASE = EPV2|U, where rtPV2iu is calculated according to paragraph (g)(2)(iii)(A)(3) of this section. 

(3) Emissions from storage vessels shall be determined as follows: 

(i) Uncontrolled emissions from Group: 1 storage vessels, ESli„, 6hall be calculated according to the equation in 

paragraph (f)(3)(i) of this section. 

(ii) The following procedures and equations shall be used to calculate actual emissions from Group 1 storage vessels, 

ESliAcniAL. 

(A) If a Group 1 storage vessel is controlled using a technology with an approved nominal efficiency greater than 

95 percent or a pollution prevention measure achieving greater than 95 percent emission reduction; 

Nominal efficiency. % 

ESli ACTUAL- ES luJi- i 

100% 

(B) Except es provided in paragraph (g)(3)(ii)(c) of this section, the nominal efficiency shall be determined as described 

in paragraph (h) of this section for a control device and paragraph (i) of this section for a pollution prevention measure. 

(C) if a Group 1 Storage Vessel is controlled using a closed vent system and control device that is demonstrated 

to achieve et least 98 percent emissior) reduction, then the 88 percent can be used as the nominal efficiency, in the 

equation in paragraph (g)(3)(ii)(A) of this section, and the bwner or operator is not required to apply for a nominal 

efficiency according to paragraph (h) of this section. 

(1) To demonstrate that 98 percent emission reduction is achieved, the owner or operator shall conduct a performance 

test according to the procedures in §63.116 of this Subpart or use a design analysis. If a performance test is used, 

sampling sites shall be located at the inlet and outlet of the control device. 

. [2) This owner or operator shall report the.results of the perfonnance: test and establish the range for the monitored 

parameters) in the Notification ;of Compliance Status required by § 63.152(b) of this subpart.

 : 

(iii) The following procedures shall be used to calculate actual emissions from Group 2 storage vessels, ES2IACIVAL: 

(A) If a Croup 2 storage vessel is controlled using a closed vent system and control device or a pollution prevention 

measure achieving a percent reduction less than or equal to the 95 percent reduction level associated widi. the;reference 

i control technology. 

Percent reduction (

t n \ 

1 - —. — ) 

100% / 

where £Siu is calculated according to the equations and procedures in paragraph (f)(3)(i) of this section. 

(B) If a Group 2 storage vessel is controlled with an internal or external floating roof, ES2iAcniAL shall be calculated 

as specified in paragraph (f)(3)(iii) or (f)(3)(iv) bf this section. 

. (C) If. a Group 2 storage vessel is controlled .using a technology with an approved nominal efficiency greater than 

95 percent or a pollution prevention measure achieving greater than 95 percent reduction. 
P.34 

:er / VbJ. 58, No. 37 / Friday, February 26, 1993 /Corrections 

ES2, ACTUAL = ES21U: l 

( ' 

Nominal efficiency % 

100% : 

(J) The nominal efficiency for a 

control device shall be determined as 

described in paragraph (h) of this 

section, except as provided in paragraph 

(g)(3)(iii)(D) of this section. 

(2) The nominal efficiency for a 

pollution prevention measure shall be 

determined as described in paragraph (i) 

of this section. 

(D) If a Group 2 Storage Vessel is 

controlled using a closed vent system 

and control device that is demonstrated 

to achieve at least 98 percent emission 

reduction, then the 98 percent can be 

used as the nominal efficiency in the 

equation in paragraph (g)(3)(iii)(C) of 

this section, and the owner or operator 

is not required to apply for a nominal 

efficiency according tb paragraph (h) of 

this section. .•-•• -

(1) To demonstrate that 98 percent 

emission reduction is achieved, the 

owner or operator shall conduct a 

performance test according to the 

procedures in § 63.116 of this Subpart or 

use a design analysis. If a performance 

test is used, sampling sites shall be 

located at the inlet and outlet ofthe 

control device. 

(2) The owner or operator shall report 

the results of the performance test and 

establish the range for the monitored 

parameter(s) in the Notification of 

Compliance Status required by 

§63.152(b) of this Subpart. 

(iv) Emissions from Group 2 storage 

vessels at baseline, ES2iBASE> shall be 

calculated as follows: 

(A) If the vessel was not controlled 

with an internal floating roof, an 

external floating roof, a closed vent 

system arid control device, or another 

control technique on November 15, 

1990, ES2JBA.SE = ES2|H and shall be 

calculated according to the procedures 

and equations in paragraph (f)(3)(i) of 

this section. 

(B) If the storage vessel was controlled 

on November 15,1990, and this control 

was not applied under either the 33/50 

or the early reduction program and was 

not the result ofa pollution prevention 

measure, 

(J) The equations in paragraph 

(f)(3)(iii) of this section shall be used to 

calculate ES2(BASE for vessels controlled 

with an internal floating roof. 

(2) The equations in paragraph 

(f)(3)(iy) of this section shall be used to 

calculate ES2JBASE for vessels controlled 

with an external floating roof. 

(73) The following equations shall be 

used to calculate ES21BASE for vessels 

controlled with a closed vent system 

and control device, 

ES2JBASE= ES2j, (>-. 

Percent reduction % 

100% 

where ESto is calculated according to the equations in paragraph (f)(3)(i) of this section. , 

(4) Emissions from transfer racks shall be determined as follows: 

(i) Uncontrolled emissions from Group 1 transfer racks, ETRlio, shall be calculated as described in paragraphs (f)(4)(i), 

(f)(4)(ii), arid (f)(4)(iii) of tbis section. 

(ii) Tbe foliowing procedures and equations shall be used to calculate actual emissions from Group i transfer racks, 

ETRIIACTUAL: • • .'.••"• ' . 

(A) If a Group 1 transfer rack is controlled using a technology, other than the reference contro) technology, with 

an approved nominal efficiency greater than 98 percent or a pollution prevention measure 7 achieving greater than 98 

percent emission reduction, 

ETRliAcruAL= ETRliu 1 

Nominal efficiency 

100% 

(B) The nominal efficiency shall be detennined as described in paragraph (h) of this section for a coatrol device 

otber than the reference technology and paragraph (i) of this section for a pollution prevention measure. 

(C) Combustion .devices, carbon adsorbers, absorbers, iand condensers-shall not -'be attributed a -nominal efficiency 

greater than 98 percent •,-•••.. • • •.'-,•.-.• . ';. 

(iii) The following procedures anal! be used to calculate actual emissions irom Group 2 .transfer racks,' ETOaucruAL: 

I (A) If a Qroup^S ts^s^te ^^.ist-contfwlled by & >cont^ GcWoving a 

percent reductions less them oe equal to the 98). percent; level assodated witb the reference control technology,' " 
P.35 

11700 Federal Register / Vol. 58, No. 37 / Friday. February 26. 1993 /. Corrections 

ETR2IACTUAL= ETR2i 

(•-

Percent reduction \ 

100% 

(1) ETR^u shall be calculated according to the equations and procedures in paragraphs (f)(4)(i). (f)(4)(ii). and (f)(4)(iii) 

of this section. 

(2) The percent reduction shall be calculated according to the procedures in paragraph (f)(4)(iv){B) (1) and (2) of 

this section. 

(B) If e Croup 2 transfer rack is controlled using a technology, other than the reference control technology, with 

an approved nominal efficiency greater then 88 percent or a pollution prevention measure achieving greater than 98 

percent reduction. 

ETR2, ACTU AL= ETR2,iJi U I 

Nominal efficiency 7 

100% 

(?) The nominal efficiency shall be determined as described in paragraph (h) of this section for a control device 

or in paragraph (i) of this section for a pollution prevention measure. 

(2) Combustion devices, carbon adsorbers, absorbers, and condensers shall not be attributed a nominal efficiency 

greater than 98 percent 

(iv) Emissions from Group 2 transfer racks at baseline, fclK2mASE. shall be calculated as follows: 

(A) If the transfer rack was uncontrolled on November 15. 1990, ETR2JBASE = ETR2iu and shall be calculated according 

to the procedures and equations in paragraphs (f)(4)(i). (f)(4)(H), and (fl(4)(iii) of this sectiori. 

(B) If the transfer rack was controlled'on November 15, 1990, and this control was not applied 7 under either the 

33/50 or the early reduction program and was not the result ofa pollution prevention measure. 

ETR2iaASE= ETR21U l -

Percent reduction 

100% 

where ETR2,„ is calculated according to tha 

equations in paragraphs (f)(4j(i), (fi(4)(ii). end 

(0(4!(<ii) of this section. Percent reduction 

shall be calculated according to the 

procedures in paragraphs (f)(4)(iv)(B)( 1) and 

(2) of this section. • 

(5) Emissions from wastewater shall 

be determined as follows. In paragraph 

(g)(5) of this section, the terms 

wastewater and wastewater stream are 

used to mean process wastewater. 

(i) EWW1« shall be calculated 

according to the equation for EWW* in 

paragraph (f)(5)(i) of this section.. 

(ii) EWW2iBASE shall be calculated 

according io the equation for 

EWWtAcruAL in paragraph (f)(5)(ii) of 

this section for each wastewater stream 

(i), which, on the baseline date specified 

in paragraph (g)(1) of this section; was ..-; 

untreated, or which was managed either 

in a wastewater tank, surface, 

impoundment, container, individual 

drain system or oil-water separator not 

meeting the requirements of §63.133 

through § 63.137 of this subpart. .. 

respectively, or in any other waste . 

management unit or treatment process 

not meeting the requirements of 

§ 63.138(h) of this subpart. 

(iii) EWVV2iaASE shall be calculated 

according to the equation for 

EVVWiAcruAL in paragraph (f)(5)(iii) of 

this section for each wastewater stream 

(i). for which all tanks, surface 

impoundments, containers, individual 

drain systems and oil-water separators 

used to manage the wastewater stream 

met the requirements of §63.133 

through § 63.137 of this subpart, 

respectively, and for which all other 

waste management units or treatment 

processes used to manage the 

wastewater stream met the requirements 

of § 63.138(h) of this subpart on the 

baseline date specified in.paragraph 

(g)(1) of this section. . .. .. , 

(iv)EVvlV2iAcTUAL shall be calculated 

as follows: 

(A) EWW2iAovAL shall be calculated 

according to tbe equation for 

EWWIACHJAL iri paragraph (f)(5)(iii) of . 

this section for each wastewater stream 

(i) which is controlled to a level less 

stringent than, or equivalent to, the 

reference control technology level. 

Group 2 streams are not considered to 

be controlled if they are not treated by 

a treatment process, or if they ere 

managed in any wastewater tank, 

surface impoundment, container, 

individual drain system, or oil-water 

separator not meeting the requirements 

of £63.133 through §63.137 of this 

subpart, respectively, or in any other 

waste management unit pr treatment 

process not meeting the requirements of 

§ 63.138(h) of this subpart. 

(B) If a Group 2 wastewater stream is 

controlled to a level more stringent than 

the level of the reference control 

technology, the procedures for 

calculating EWWIIACIUAL in. paragraph,, 

(g)(5)(vj of this section shall be used to 

calculate EWWiiAcruAL.: , 

(v) The following equations for 

EWWliACTUAL shall be used to calculate 

emissions from each Group 1 

wastewater stream (i) that is controlled 
P.36 

Federal Register / Vol. 58, No. 37 /Friday, February 26, 1993 / Corrections 11701 

to a level more stringent than the 

reference control technology. Group 1 

streams are not considered to be 

controlled to or above the level of the 

reference control technology if they are 

managed in any wastewater tank, 

surface impoundment, container, 

individual drain system, or oil-water 

separator not meeting the requirements 

of §63.133 through §63.137 of this 

subpart, respectively, or in any other 

waste management unit or treatment 

process not meeting the requirements of 

§ 63.138(h) of this subpart. 

(A) If the Group 1 wastewater stream 

(i) is controlled using a treatment 

process or series of treatment processes 

which achieve an approved nominal 

reduction efficiency in the total VOHAP 

concentration of stream (i) greater than 

that which would be achieved using the 

design steam stripper specified in 

§ 63.138(f) of this Subpart, but the 

control device used to reduce HAP 

emissions from the vapor strsam(s) 

vented from the treatment process(es) 

achieves sn efficiency equal to the 95 

percent of the reference control 

technology, the following formula shall 

be used: 

EW\V1IACTUAI = (6.0 x 10-* )Q,H, I | Fen!H APmi( 1 

m= i 

PR,m)] +0.05 (6.0xlO-K)Q,H, I [HAPimPRim] 

m =l 

where all terms are as defined and detennined in paragraph (f)(5) of this section. 

(B) If the Group 1 wastewater stream (i) is not controlled using a treatment process or series of treatment processes 

which achieves a total VOHAP concentration reduction greater than that which would be achieved using the design 

steam stripper specified in § 63.138(f) of this Subpart, but the vapor stream(s) vented from the treatment process(es) 

are controlled using a device, other than the reference control technology, fpr which EPA has approved a nominal 

efficiency greater than 95 percent, the following formula shall be used: 

EWWl,AC1UAly 7 6.0 x 10~s)Q,H, I. [ Femli APl!71(. 1 - Frm); 

niFl 

Nomina! efficiencv % s 

V 

100 

(6.0xl()-K)Q1H, I |HAPimFrm| 

m =l 

where all terms other than nominal 

efficiency are as defined and 

determined in paragraph (f)(5) of this 

section. 

(C) If the Group 1 wastewater stream 

(i) is controlled using a treatment 

process or series of treatment processes 

which achieves a total VOHAP 

concentration reduction greater than 

that which would be achieved using the 

design steam stripper specified in 

§63.138(f) of this Subpart, and the 

vapor stream(s) vented from the 

treatment process are controlled using a 

device, other than the reference control 

technology, with an approved nominal 

efficiency greater than 95 percent, the 

following formula shall be used: 

EWWIlACTlML= (6.0xl()-K)Q,H, I [FemHAP,m( I -PR„,)J 

m=l 

( -

Nominal efficiency % 

100 ) 

(6:0xl()-»)Q,HI I [HAPimPRm| 

m =l 

where all terms other than nominal 

efficiency are as defined and 

determined in paragraph (f)(5) of this 

section. 

(D) The nominal efficiency for a 

treatment process or control device shall 

be determined as described in paragraph 

(h) of this section. 

(h) The following procedures shall be 

followed to establish a nominal 

efficiency for any control technology 

achieving greater emission reduction 

than the percentage efficiency assigned 

to the reference control technology in 

§ 63.111 of this subpart. The procedures 

in paragraphs (h)(1) through (h)(5) of ... 

this section shall be followed for control 

technologies that are different in use or 

design from the reference control 

technologies. The procedures in 

paragraph (h)(6) of this section shall be 

followed for process vents controlled by 

reference control technologies that can 

be demonstrated to consistently achieve 
P.37 

1170 2 Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

a higher control efficiency than that 

which hss been assigned by the 

proposed rule to that particular type of 

device. 

(1) The owner or operator seeking 

permission to take credit for use of a 

ttxhnology that is different in use or 

design from the reference control 

technology shall submit the information 

specified in paragraphs (h)(l)(i) through 

(h)(l)(iv) of this section in writing to the 

Director of the EPA Office of Air Quality 

Planning and Standards: 

(i) Emission stream characteristics of 

each emission point to which the 

control technology is or will be applied 

including the kind of emission points, 

flow, organic HAP concentration, and 

all other stream characteristics 

necessary to design the control 

technology or determine its 

performance, 

(ii) Description of tiie control 

technology including design 

specifications. 

(iii) Documentation demonstrating to 

the Director's satisfaction the control 

efficiency of the control technology. 

This may include performance test data 

collected using an appropriate EPA 

method or any other method validated 

according to Method 301 of appendix A 

of this part, lf it is infeasible to obtain 

test data, documentation may include a 

design analysis and engineering 

calculations. The basis ofthe 

calculational procedures and all inputs 

and assumptions made in the 

calculations shall be documented. 

(iv) A description ofthe parameter or 

parameters to be monitored fo ensure 

that the control technology will be' 

operated in conformance with its design 

and an explanation of the criteria used 

for selection of that parameter (or 

parameters). 

(2) The Director shall determine 

within 120 days whether an application 

presents sufficient information to 

determine nominal efficiency. The 

Director reserves the right to request 

specific data in addition to the items 

listed in paragraph (h)(1) of tliis section. 

(3) The Director shall determine 

within 120 days ofthe submittal of 

sufficient data whether a device shall 

havo a nominal control efficiency and 

the level of that nominal efficiency. If, 

in tho Director's judgment, the control 

technology achieves a level of emission 

reduction greater than the reference 

control technology for a particular kind 

of emission point, the Director will 

publish a Federal Register notice 

establishing a nominal efficiency for the 

control technology. . 

(4) The-Director may condition 

permission to take emission credits for 

uso of the control technology on 

requirements that may be necessary to 

ensure operation and maintenance to 

achieve the specified nominal 

efficiency. 

(5) In in ose cases where the owner or 

operator is seeking permission to take 

credit for use ofa technology lhat is -

different in use or design from the 

reference control technology and the 

different technology will be used in no 

more than three applications, the 

information listed in paragraphs (h)(l)(i) 

through (h)(l)(iv) can be submitted to 

the operating permit authority for the 

source instead of the Director. In these 

instances, use and conditions for use of 

the different technology can be 

approved as part of an operating permit 

application or modification. In these 

instances, a Federal Register notice Is 

not required to establish the nominal 

efficiency for the different technology. 

(i) If, in reviewing the application, the 

operating permit authority believes the 

technology has broad applicability for 

use by other sources, the authority shall 

submit the information provided in the 

application to the Director of the EPA 

Office of Air Quality Planning and 

Standards. The Director shall review the 

technology for broad applicability and 

may publish a Federal Register notice; 

however, this EPA review shall not 

affect the operating permit authority's 

approval of the nominal efficiency of 

the technology for the specific 

application. 

(ii) If, in reviewing an application for 

a process vent control, the operating 

permit authority determines that the. 

technology is not different in use and 

design from the reference control 

technology, the authority shall submit 

the application to the Director ofthe 

EPA Office of Air Quality Planning and 

Standards. The procedures in paragraph 

(h)(6) of this section shall be followed 

for submission of information, review, 

and approval of the nominal efficiency. 

If, in reviewing an application for a 

control for an emission point other than 

a process vent, the operating permit 

authority determines the technology is 

not different in use or design from the 

reference control technology and is not 

a closed vent system fbr a storage vessel, 

the authority shall deny the application! 

(6) An owner or operator seeking 

permission to take credit for a process 

vent using reference control technology 

that achieves a percent emission 

reduction efficiency higher than the 

percent assigned to the reference control 

technology in § 63.111 shall submit the 

information in paragraphs (h)(8)(i) 

through (h)(6)(iv) of this section to the 

Director of the EPA Office of Air, Quality 

Planning and Standards. The 

procedures in paragraphs (h)(2) through 

(h)(4) of tbis section shall be followed 

for review and approval of the nominal 

efficiency of the control-technology in 

the specified application. 

(i) emission.stream characteristics of 

each process vent to which the control 

technology is or will be applied 

including the flow, organic HAP 

concentration, and all other vent stream 

characteristics necessary to design the 

control technology or determirie its 

performance. 

(ii) Description ofthe control 

technology including design 

specifications, 

(iii) Documentation demonstrating to 

the Director's satisfaction that the 

technology in the intended application 

achieves 99.9 percent or greater 

emission reduction. This documentation 

shall include performance test data 

collected using an appropriate EPA 

method or any other method or data 

validated according to Method 301 of 

appendix A of this part. 

(iv) A plan for instituting continuous 

emissions monitoring to demonstrate 

that 99.9 percent emission reduction is 

achieved on a continuous basis. 

(i) The following procedures shall be 

used for calculating the efficiency 

(percent reduction) of pollution 

prevention measures: 

(1) A pollution prevention measure is 

any practice which meets the criteria of 

paragraphs (i)(l)(i) and (ii) of this 

section. 

(i) A pollution prevention measure is 

any practice which results in a lesser 

quantity of organic HAP emissions 

released to the atmosphere prior to outof-process recycling, treatment, or 

control of emissions, while the same 

quantity ofthe same product is 

produced. 

(ii) Pollution prevention measures 

may include substitution of non-toxic 

for toxic feedstocks in making a 

product; alterations to the production 

process to reduce the volume of 

materials released to the environment; 

equipment modifications; housekeeping 

measures; and in-process recycling that 

returns waste materials directly to 

production as raw materials. 

(2) The emission reduction efficiency 

of pollution prevention measures 

implemented after 1987 can be used in 

calculating the actual emissions from an 

emission point in the debit and credit 

equations in § 63.150 (0 and (g) of this 

subpart. 

(i) For pollution prevention measures, 

the percent reduction used in the 

equations in paragraphs (f)(2), (f)(3), 

(f)(4), and (f)(5) of this section, and 

paragraphs (g)(2), (g)(3). (g)(4). and (g)(5) 

of this section, is the percent difference 

between the monthly organic HAP 
Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 /Conection s 11703 

emissions for each emission point after 

the pollution prevention measure for the 

most recent month versus monthly 

emissions from the same emission point 

before the pollution prevention 

measure, adjusted by the volume of 

product produced during the two 

monthly periods. 

(ii) The following equation shall be 

used to calculate the percent reduction 

of a pollution prevention measure for 

each emission point. 

EB = Z [(6.0xlO-8)QBiHnii: Fe^HAPoin, 

i = l - m= l 

where: 

Percent reduction=Efficiency of pollution prevention measure (percent organic HAP reduction). 

EB=Monthly emissions before the pollution prevention measure, determined as specified in paragraph (i)(2)(ii) (A), (B), 

and (C) of this section. 

Epp=Monthly emissions after the pollution prevention measure, as determined for the most recent month, detennined 

as specified in paragraph (i)(2)(ii)(C) or (D) of this section. 

PB=Monthly production before the pollution prevention measure, during the same period over which EB is calculated. 

Ppp=Monthly production after the pollution prevention measure, as determined for tha most recent month. 

(A) The monthly emissions before the pollution prevention measure, EB, shall be determined in a manner consistent 

with the equations and procedures in paragraphs (f)(2), (f)(3), and (f)(4) of this section for process vents, storage vessels, 

and transfer operations. 

(B) For wastewater, EB shall be calculated as follows. In paragraph (i)(2)(ii)(B) of this section, the terms wastewater 

and wastewater stream are used to mean process wastewater. 

(EpPxPn) 

Percent reduction =• 

pp 

•Bxl00% 

where: 

n=Number of wastewater streams. 

QHi=Average flow rate for wastewater stream (i) before the pollution prevention measure, as determined by the procedure 

in § 63.144(e)(3) of this Subpart, liters per minute, before implementation of the pollution prevention measure. 

HBi=Number of hours per month that wastewater stream (i) was discharged before the pollution prevention measure, 

hours per month. 

s=Total number of organic HAP compounds in wastewater stream (i). 

Fem=Fraction emitted of HAP compound (m) in wastewater from Table 33 of this Subpart, dimensionless. 

HAPmm=Average organic HAP concentration of compound (m) in wastewater stream (i), defined and determined according 

to paragraph (f)(5)(i) of this section/before the pollution prevention measure, in parts per million by weight, 

as measured before the implementation ofthe pollution measure. 

(1) Values for Qai and HAPBim may be determined during an initial performance test conducted under representative 

conditions, or 

(2) Values for Qw may be determined from records as specified in § 63.144(a) of this subpart, and values for HAPBim 

may be determined through process knowledge as specified in § 63.144(b) of this subpart. 

(C) If the pollution prevention measure was implemented prior to the effective date of the reguletion, records moy 

be used to determine EB. 

(D) The monthly emissions after the pollution prevention measure, Epp, may be determined by testing or by design 

analysis and documented engineering calculations. Once an emissions to production ratio has been established, this 

can be used to estimate monthly emissions from monthly production records. 

(E) For wastewater, Epp shall be calculated using the following equation. In paragraph (i)(2)(ii)(E) of this section, 

the terms wastewater and wastewater stream are used to mean process wastewater. 

EpP = I [ (6.0 x IO"8)QPpiHppi I FenJiAPpp,TM | 

> = ' 1 m= l J 

m 

where: 

n, Qppj, Hppj, s, Fem, and HAP,^ 

defined and determined as 

are 

described above under the 

definition of EB. except that Qppi. 

Hppi, and HAPppim shall be -

determined after the pollution 

prevention measure has been 

implemented. 
11704 Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

P.39 

(iii) All equations, calculations, test 

procedures, test results, and other 

infonnation used to determine the 

percent reduction achieved by a 

pollution prevention measure for each 

emission point shall be fully 

documented. 

(iv) The same pollution prevention 

measure may reduce emissions from 

multiple emission points. In such cases, 

the percent reduction in emissions for 

each emission point must be calculated. 

(v) For the purposes of the equations 

in paragraphs (g)(2). (g)(3), (g)(4), and 

(g)(5) of this section, used to calculate 

credits for emission points controlled 

more stringently than the reference 

technology in paragraphs (g)(2), (g)(3). 

(g)(4), and (g)(5) of this section, the 

nominal efficiency of a pollution 

prevention measure is equivalent to the 

percent reduction ofthe pollution 

prevention measure. When a pollution 

prevention measure is used, the owner 

or operator of a source is not required 

to apply to the Director for a nominal 

efficiency and is not subject to 

paragraph (h) of this section. 

TABLE 20.—AVERAGE STORAGE TEMPERATURE (Ts) AS A FUNCTION OF TANK 

PAINT COLOR 

Tank color 

White ....... 

Aluminum. 

Gray 

Black 

Average Storage Temperature (Ts) 

TAM> 

T A *2^ 

TA+3.5 

TA+5.0 

* T A is the averaae annual ambient 

temperature in degrees Fahrenheit. 

TABLE 21.—PAINT FACTORS FOR FIXED ROOF TANKS 

Tank color 

Roof Shell 

Paint Factors (Fp) paint 

condition 

Good Poor 

White 

Aluminum (specular) 

White ..... 

Aluminum (specular) 

White 

Aluminum (diffuse)... 

White 

Light gray 

Medium gray 

White 

White 7... 

Aluminum (specular) 

Aluminum (specular) 

Aluminum (diffuse) ... 

Aluminum (diffuse) ... 

Gray 

Ught gray — 

Medium gray 

1.00 

1.04 

1.16 

1.20 

1.30 

1.39 

1.30 

1.33 

1.40 

1.15 

1.18 

1.24 

1.29 

1.38 

1.46 

1.38 

1.44 

1.58 

TABLE 22:—AVERAGE CLINGAGE FACTORS (C)* 

Liquid 

Shell condition 

Light rust* Dense rust G unite 

lined 

Gasoline 

Single component stocks 

Crude oil _ 

0.0015 

0.0015 

0.0060 

0.0075 

0.0075 

0.030 

0.15 

0.15 

0.60 

•Units for average dirigage factors are barrels per 1.000 square feeL 

if no specific information ts available, these values can be assumed to represent the most common condition of tanks currently In use. 

TABLE 23.—TYPICAL NUMBER OF COLUMNS AS A FUNCTION OF TANK DIAMETER FOR INTERNAL FLOATING ROOF TANKS 

WIT H COLUMN SUPPORTED FIXED ROOFS* 

Tank diameter range (D In feet) 

Typical 

number of 

columns. 

(Nc) 

0<D585„ . 

65<D 5 100 ... 

100 < D 5 120 ... 

120 < D S 135 ... 

135 < D 5 150 ... 

150<DS170 ... 

170<D 5 190 ... 

190 < D 5 220 ... 

220 < D 5235 ... 

235 < D 5 270 ._ 

270 < D 5 275 ... 

275 < D 5 290 ... 

290<D5330 ... 

330 < D 5360 ... 

360 < D 5400 .-

1 

6 

7 

8 

9 

16 

19 

22 

31 

37 

43 

49 

61 

71 

81 

* Oata in this table should not supersede information on actual tanks. 
P.40 

Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 11705 

TABLE 24.—EFFECTIVE COLUMN DIAMETER (Fc) 

Column type Fc 

(feet) 

9-inch by 7-Inch built-up columns 

8-lnch-diametor pipe columns 

No construction details known .... 

1.1 

0.7 

1.0 

TABLE 25.—SEAL RELATED FACTORS FOR INTERNAL FLOATING ROOF VESSELS 

Seal type Ks 

Liquid mounted resilient seal: 

Primary seal only : _ 

With rim-mounted secondary seal • :..... « ;.... 

Vapor mounted resilient seal: 

Primary seal only 7 

With rim-mounted secondaiy seal* 

'if vessel-specific infonnation is not available about the secondary seal, assume only a primary seal is present 

3.0 

1.6 

6.7 

2.5 

TABLE 26.—SUMMARY OF INTERNAL FLOATING DECK FITTING LOSS FACTORS (KF) and Typical Number of Fittings 

(NF) 

Deck fitting type Deck fitting loss factor Typical number of fittings (Nr) 

Access hatch ; 

Bolted cover, gasketed 

Unbolted cover, gasketed 

Unbolted cover, ungasketed 

Automatic gauge float well .„ _„ _ 

Bolted cover, gasketed 

Unbolted cover, gasketed 

Unbolted cover, ungasketed 

Column well 

Buittup column-sliding cover, gasketed 

Buittup column-sliding cover, ungasketed 

Pipe column-flexible fabric sleeve seal 

Pipe column-sliding cover, gasketed 

Pipe column-sliding cover, ungasketed 

Ladder well -

Sliding cover, gasketed 

Sliding cover, ungasketed 

Roof leg or hanger well 

Adjustable .._ :....... 

Fixed ... 

Sample pipe or well 

Slotted pipe-sliding cover, gasketed 

Slotted pipe-sliding cover, ungasketed 

Sample well-slit fabric seal, 10 percent open area 

Stub drain, 1-ln diameter"..; 

Vacuum breaker : „ 

Weighted mechanical actuation, gasketed 

Weighted mechanical actuation, ungasketed 

1.6 

11 

b25 

5.1 

15 

»28 

33 

c47 

10 

19 

32 

(') 

56 

"76 

"7.9 

0 

«(5+D/10+D2/600) 

44 

57 

»12 

1.2 e

(D2/125) 

1 

»0.7 

0.9 

•Units for KP are pound-moles per year. ... 

"If no specific information is available, this value can be assumed to represent the most common/typical deck fittings currently used. 

c

 D=Tank diameter (feet). 

d

 Not used on welded contact internal floating decks. 

"See Table 23. 

TABLE 27.—DECK SEAM LENGTH FACTORS" (SD) FOR INTERNAL FLOATING ROOF TANKS 

Deck constmction 

Typical 

deck 

seam 

Continuous sheet construction? 

5-feet wide sheets _. 

6-feet wide sheets. 

7-feet wide sheets _....__. 

«0.2 

0.17 

0.14 
P.41 

11706 Federal Register / Vol. 58.: No. 37 / Friday, February 26, 1993 / Corrections 

TABLE 27.-T-DECX SEAM LENGTH FACTORS" (SD) FOR INTERNAL FLOATING ROOF TANKS—Continued 

Deck construction 

Typical 

deck 

seam 

Panel construction" 

5x7.5 feet rectangular. 

5x12 feet rectangular. 

0.33 

0.28 

"Deck 6eamloss appUes to bolted decks only.- Units tor Su are feet per square feet 

«

,So=1/W. where Wtsheet width (feet). 

c

ll no specific Information b avaiiabie, these factors can be assumed to represent the most common bolted decks currently In use. 

0So=:(L*W)/LW, where W=panel width (feet), and L=panel length (feet). 

TABLE 28.—SEAL RELATED FACTORS FOR EXTERNAL FLOATING ROOF VESSELS 

Sea) type 

Welded vas7 sels 

Ks 

71.2; 

0.8: 

i

0

-

2

.; 

1.1 

0.8 

.0.7 

A 2 

- 0.9 

70.2 

N 

1.5 

172 

1.0 

1.0 

0.9 

0 4 

2.3 

22 

2.6 

Riveted vessels . 

Ks 

1.3 

1.4 

0.2 

•NA 

. NA 

NA 

-NANA 

NA 

N 

. 1 5 

1.2 

1.6 

NA 

. NA 

NA 

NA 

. NA 

. NA 

Metallic shoe seal: 

Primary seal only .,. 

With shoe-mounted secondary seal 

With rim-mounted secondary seal.. 

Uquid mounted resilient seal: 

Primary seal only 

With weather shield 

With rim-mounted secondary seal 

Vapor mounted resilient seal: 

Primary seal only ;......... 

With weather shield 

With rim-mounted secondary seal.. 

»NA=Not applicable. 

TABLE 29.—ROOF FITTING LOSS FACTORS," KF „ Kn,, AND M. AND TYPICAL NUMSER OF ROOF FITTINGS. N T 

Fitting type and construction details 

Loss factors6 

Kr. (tb-mole/yr) :Krt(!bHnola/(ml/ 

br)°>-y

r

) 

m . 

(dimensionless) 

Typical number of fittings, 

'. Nr . 

Access hatch (24-ln-diaroeter well) ..... 

Bolted cover, gasketed 

Unbolted cover, ungasketed 

Unbolted cover, gasketed .....;.... 

Unslotted guide-pole well (8-in-diameter unstotted pola, 

21-ln-diamsler well). 

Ungasketed sliding cover ..... 

Gasketed sliding coyer .......:...... ... 

Slotted gukJa-pola/sample well (8-hvdiameter unslotted 

pole. 21-Jn-dlameter well). 

Ungasketed sliding cover, without float 

Ungasketed sliding cover, with float : 

Gasketed sliding cover, without float 

'Gasketed sliding cover, with float r. 

Gauge-float well (20-ihch diameter) 

Unbolted cover, ungasketed 

Unbolted cover, gasketed 

Bolted cover, gasketed :...; 

Gauge-hatch/sample well (8-inch diameter) ......... , 

Weighted mechanical actuation, gasketed 

Weighted mechanical actuation, ungasketed 

Vacuum breaker (10-inch-diameter well) 

Weighted mechanical actuation, gasketed 

Weighted mechanical actuation, ungasketed 

Roof drain (3-Inch diameter) ...; 

Open 

90 percent ciosed 

Roof leg (3-inch diameter) 

Adjustable, pontoon area 

Adjustable, center area _ _ 

0 

2.7 

2.9 

.5 

025 

0 

7.1 

0.41 

0 

0 

0 

0 

0 

0 

2.3 

2.4 

0 

0.95 

0.91 

\2 

\2 

0 

0.51 

6.7 

3.0 

310 

29 

260 

8.5 

5.9 

0.34 

0 

0.14 

2.4 

0.17 

3.0 

7.0 

0.81 

0.20 

0.06 

(

c

)0 

1.0 

1.0 

0.98 

(

c

) 

1.2 

2.0 

\2 

24 

(

c

)10 

1.0 

0 

(

c

)io 

1.0 

(

c

)io 

1.0 

io 

n 

N« (Table-30). 

Nrr (Table-30). 

(

c

)14 

Nm (Table-310. 

«1.0 

«1.0 
Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 11707 

TABLE 29.—ROOF FITTING LOSS FACTORS,»:KF»IW AND M* AND TYPICAL NUMBER OF ROOF FITTINGS, NT-rContJnued 

Rtting type and construction details 

Fixed 

Fixed „ 

Rim vent (6-Inch diameter) 7 

Loss factors" 

KF. (Ib-mole/yr) 

.0 

1.7 

0.41 

0.41 

0 

0.71 

0.68 

KFb(U>mole/Imi/ 

hr)»-yr) 

0.06 

.7 

0 

0 

0 

0 

0.10 

1.8 

m 

(dimensionless) 

0 '-. 

; oooo 

c

1.0 

1.0 

Typical number of fittings, 

Nr 

Nr a (TabkH310-

'«1. 

•The roof fitting loss factors, KF., Kn>, and m, may only be used for wind speeds from 2 to 15 miles per hour. 

-" Unit abbreviations are as follows: to=pouRd; mi=miles; hr=hour; yrs=year. 

«lf no specific information is avaiiabie, this value can be assumed to represent the most common or typical roof fittings currently in use. 

'A slotted guide-pole/sample well is an optional fitting and is not typically used. 

• Roof drains that drain excess rainwater Into the product are not used on pontoon floating roofs. They are, however, used on double-deck 

floating roofs and are typically left open. 

'The most common roof leg diameter is 3 inches. The loss factors for Vh Inch cfiameter roof legs are provided for use If this smatler size roof 

Is used on a particular floating roof. . . t 

. « Rimvents are used only with; mechanical-shoe primary seals. 

; TABLE 30.—TYPICAL NUMBER OF VACUUM BREAKERS, NFS AND ROOF DRAINS," N n 

Tank diameter D (feet)'* 

50 

100 

150 

200 

250 

300 

350 

400 

No. of vacuum breakers, N » 

Pontoon roof 

1 

1 

2 

3 

4 

5 

.6. 

7 

Double-deck roof 

1 

1 

2 

2 

3 

3 

' 4 

4 

No. of roof drains, N n (doubledeck roof)c 

1 

1 

2 

3 

5 

7 

d 

d 

•TThis table should not supersede Information based on actual tank data. : 

"If the actual diameter is between the diameters.Isted, the closest diameter listed should be used: If the actual diameter Is midway between 

the diameters listed, the next larger cfiameter should be used. : 

cRoof drains that drain excess rainwater into the product are hot used on pontoon floating roofs. They are, however, used on double-deck 

floating roofs, and are typically left open. 

"For tanks more than 300 feet In diameter, actual tank data or the manufacturer's recommendations may be needed for the number of roof 

drains. .; • . \ 

Tank diameter D (feet)* 

30 

40 

50 

1

 60 

70 

80 

, 9 0 

100 

110 

i 120 

: 130 

• 140 

. 150 

7 160 

170 

, 180 

7 190 

200 

7 210 

-r 220 

230 

TABLE 31;—TYPICAL NUMBER OF ROOF LEGS," Nra 

Pontoon roof 

No. of pontoon legs 

4 

4 

6 

9 

13 

15 

16 

17 

18 

19 

20 

21 

23 

26 

27 

-...28 

29 

30; 

7 31 

i 32 

: . 33 

Na of center legs 

2 

4 

6 

7 

9 

10 

12 

16 

20 

24 

28 

33 

38 

42 

49 

56 

62 

69 

77 

> 83 

92 

No. of legs on double-deck roof 

6 

7 

8 

10 

13 

16 

20 

- -...•• ' 25 

29 

34 

40 

46 

• 62 

• . /68 

66 

..-,:,'..74 

82 

y 90 

. 88 

107 

116 
11708 FederalRegister / Vol. 58, No. 37 /Friday, February 26. 1993 / Corrections 

Tank cfiameter D (feet)* 

240 

250 

260 

270 

280 

290 

300 

310 

320 

330 

340 

350 

360 

370 

380 

390 

. 400 

TABLE 31.—TYPICAL NUMSER OF ROOF LEGS," NF«—Continued 

Pontoon roof 

No. of pontoon tegs 

34 

' 34 

36. 

36 

37 

38 

38 

39 

• 39 

40 

41 

42 

44 

45 

46 

47 

43 

No. of center tegs 

101 

109 

118 

128 

138 

148 

158 

168 

179 

190 

202 

213 

226 

238 

252 

256 

281 

No. of legs on double-deck root 

127 

. 138 

149 

162 

173 

186 

200 

213 

226 

240 

255 

. . 270 

285 

300 

315 

330 

345 

* This table should mot supersede information ba-sed'on adaa! lank data. 

*« the actual diameter Is between the diameters listed, iha closest diameter listed should ba used. If me actual diameter Is midway between 

the diameters listed, tfw oext.larger diameter should ba used. 

TABLE 32.—SATURATION FACTORS 

Cargo carrier 

Tank 

trucks : 

and rail 

' lank cars. 

• ' 

Mode of operation 

Submerged loading of 

a dean cargo tank. 

Submerged loading: 

dedicated noimal 

. service. 

Submerged loading: 

dedicated, vapor toal-

'""' arvce' service. 

Splash loading of a 

deari cargo tank. '" 

Splash loading: dedicated nonrial serv:

 •- • 

fee'. 

Splash loading: dedicated vapor balance 

service. 

S factor 

0.50 

0.80 

1.00 

. L45 

1;*»S 

1.00 

TABLE 33.—FRACTION REMOVED (Fr) FOA 

HAP COMPOUNDS IN WASTEWATEH 

STREAMS—Continued 

TABLE 33.—FRACTION" REMOVED (Fr) FOA 

HAP COMPOUNDS IN .WASTEWATER 

STREAMS—Conti nued 

TABLE 33.—FRACTION REMOVED'• (Fr) FOR 

HAP COMPOUNDS IN WASTEWATER" 

STREAMS 

Chemical name 

Acetaldehyda 

Acetonitrile -. 

Acstophenorie 

Acrolein 

Acryksnitrila 

Ally! chloride 

Aniline 

Benzene 

Benzyl chloride 

Biphenyl 

Bromoform 

1,3-Butadiene 

Carbon disulfide 

Carbon tetrachloride .... 

2-Chloroacetophenone 

Qtlorobenzene 

Fr1.000 

0.934 

0.920 

0.957 

0.960 

1.000 

0,468 

1.000 

1.000 

1.000 

1.000 

1.000 

1.000 

1.000 

0.939 

1.000 

Chenscalnama 

CWorofonn 

Chloroprene' (2 -Chloro-1.3-8utadiane) .' 

o-Oresol 

Cumene (isopropyl benzene) 

1,4-DicfrtiorobBnzene(p) 7...... 

•Dichloroethyl ether 

1.3-Dk£>k*r©propene ..„. 

N.N-Dimsttiyianiline 

Oiethyt sulfate. . .... 

S.S'-DimsthylbenzJdine 

Ll-Oimelhylhvdrazins .-...:.7 :..' 

• Dimethyl sulfate 

2,4-Dimirophsnol : 

2.4^lnitroto!uene : 

1.4^Dioxaria.(L4-Oieihy1eneoxlde) . 

Epichtorohydrin( 1 -Chloro-2.3-

' epoxypropane) 

; Ethyl acrylate :•..; 

Ethylbenzene .;...... 

Ethyl chloride (Chloroethana) 

Ethylene dibromide 

Ethylene dichloride -. (1.2-

Dichloroelhane) _ 

Ethylene oxide .........'.;.'...... 7... 

Ethylidene dichiorida (1.1-

Dichloroeihane) ...;..„.:.: 

Diethylene glycol dimethyl ether .... 

Ethylene glycol monomethyl ether 

acetate ; 

Ethylene glycol dimethyl elher ....... 

Diethylene glycol diethyl ether 

Ethylene glycol monobutyl ether 

acetate : 

Ethylene glycol monoethyl ether 

acetate _..::: 

HexachkHobehzene 

Hexachlorobutadiene ......Y:Y 

Hexachloroethans 

Hexane ;.-. 

Isophorone ...7.. AY. 

Fr 

1.000 

LOW) 

0.448 

LOOO 

1.000 

0.935 

LOOO 

0.927 

0.814 

0.635 

0.448 

0.697 

0.908 

0.626 

0.787 

0.690 

0.981 

1.000 

1.000 

1.000 

LOOO 

1.000 

1.000 

0.425 

0.529 

0.943 

0.523 

0.927 

0.470 

1.000 

LOOO 

1.000 

1.000 

0.945 

Chemical name 

Methanol ....; ;...-. 

Methyl bromide (Bromomethahe)... 

Methyl chloride (Chtoromelhane) ... 

Methyl chloroform (1,1,1-

Trichloroelhane) 

Methyl ethyl ketone (2-Butanone) .. 

Methyl Isobutyl ketone (Hexone).... 

Methyl methacrylate ...........: 

Methyl Jert-outyl ether ..........: 

Methylene ' chloride 

. (DichJoromalhane},:.... 

Naphthalene .... 

Nitrobenzene 

2-Nitropropana 

Phosgene .-. 

Propidnaldehyda ,. 

Propylene dichloride (1,2-Dlchloropropane) 

Propylene oxide 

Styrene ........;. „.... 

1.1.2.2-Tetrachtoroe1hane 

TetracMoroelhyiene 

(PerchloroeJhylerie) 

Toluene „:..;„'_....' ;..: 

o-Toluidine;..~. 

1.2.4-Trichlorobenzene 

1.1.2-Trichlbroethane 

Trichloroethylene 

2,4,5-Trichlorophenol 

Triethytamine ...... ; 

2,2,4:Trimeihy1pentane 

Vinyl acetate ..-.'.. ..........:,........ 

Vinyl chloride .......: 

Vinylidene . chloride (1,1-

Dichloroethylene) ....: 

m-Xylene :.......: 

o-Xylene ........7 

p-Xytene ...:..+<......... 

Fr 

0.829 

1.000 

i.ooo 

LOOO 

LOOO 

1.000 

0.958 

LOOO 

LOOO 

LOOO 

0.936 

LOOO 

1.000 

0.952 

LOOO 

LOOO 

1.000 

LOOO 

LOOO 

1.000 

0.487 

1.000 

1.000 

1.000 

0.914 

1.000 

1.000 

1.000 

1.000 

LOOO 

1.000 

i.ooo 

1.000 
P.1 

OAR Box 1252 

Prepped by Candice Davis 

Document Number: 

71) FED REG VOL. 58, NO. 37 2/26/93 

Docket Number: 

A-90-22 

Printed 5/21/2008 3:16:16 PM Sheet 71 of 184 
.y&r<j9Wl Al e A'90'3d H0tt Docfcers A'^D'ZZ^ 

P.2 

Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 11709 

ENVIRONMENTAL PROTECTION 

AGENCY 

40 CFR Part 60 

[AD-FRL-4534-4] 

Standards of Performance for New 

Stationary Sources; Appendix A—Tesfl 

Methods; Revisions to Methods 18 and 

26 and Addition of Method 26A to 

Appendix A 

Correction 

In proposed rule document 92-28293 

beginning on page 62798 in the issue of 

Thursday, December 31,1992, various 

portions of the document were illegible 

and several illustrations were 

incorrectly published at the end of the 

document. For clarification, the 

proposed rule is reprinted below. Also, 

the FR Document number appearing at 

the end of the document is correctly 

noted above. 

SUMMARY: The purpose of this action is 

to propose revisions to Method 18, 

"Measurement of Gaseous Organic 

Compound Emissions by Gas 

Chromatography" and to Method 26, 

"Determination of Hydrogen Halide and 

Halogen Emissions from Stationary 

Sources—Midget Impinger Method," 

and to propose the addition of Method 

26A, "Determination of Hydrogen 

Halide and Halogen Emissions from 

Stationary Sources—Isokinetic 

Method," to appendix A of 40 CFR part 

60. Proposed regulations published in a 

separate announcement under 40 CFR 

part 63 entitled "National Emission 

Standards for Organic Hazardous Air 

Pollutants from Synthetic Organic 

Chemical (SOCMI) Industry," include 

testing requirements for hydrogen 

halides and halogens after incineration 

control devices. Method 13 is being 

revised to clarify the phrase 

"engineering judgment" as it relates to 

choosing a sampling methodology. 

Method 26 for anisokinetic 

determination of hydrogen chloride 

emissions is being revised to add 

provisions for determining emissions of 

other hydrogen halides and halogens. 

Method 26A is being proposed as an 

isokinetic version of Method 26. 

A public hearing will be held, if 

requested, to provide interested persons 

an opportunity for oral presentation of 

data, views, or arguments concerning 

the proposed test methods. 

DATES: Comments. Comments must be 

received on or before March 31,1993. 

Public Hearing. If anyone contacts 

EPA requesting to speak at a public 

hearing by January 21,1993, a public 

hearing will be held on February 10, 

1993 beginning at 10 a.m. Persons 

interested in attending-the hearing 

should call the contact mentioned under 

ADDRESSES to verify that a hearing will 

be held. 

Bequest to Speak at Hearing. Persons 

wishing to present oral testimony must 

contact EPA by January 21,1993. 

ADDRESSES: Comments. Comments 

should be submitted (in duplicate if 

possible) to: Air Docket Section (LE131), Attention: Docket Number A-90 -

19, U. S. Environmental Protection 

Agency, 401 M Street, SW., Washington, 

DC 20460.' 

Public Hearing. If anyone contacts 

EPA requesting a public hearing, it will 

be held at EPA's Emission Measurement 

Laboratory Building, Research Triangle 

Park, North Carolina. Persons interested 

in attending the hearing or wishing to 

present oral testimony should notify 

Robin R. Segall, Emission Measurement 

Branch (MD-19), Technical Support 

Division, U.S. Environmental Protection 

Agency, Research Triangle Park, North 

Carolina 27711, telephone (919) 541 -

0893. 

Docket. Docket No. A-90-19, 

containing materials relevant to this 

rulemaking, is available for public 

inspection and copying between 8 a.m. 

and 3:30 p.m., Monday through Friday, 

at EPA's Air Docket, room M-1500,1st 

Floor, Waterside Mall, 401 M Street, 

SW.. Washington, DC 20460. A 

reasonable fee may be charged for 

copying. 

FOR FURTHER INFORMATION CONTACT: 

Terry Harrison or Robin R. Segall, 

Emission Measurement Branch (MD19), Technical Support Division, U.S. 

Environmental Protection Agency, 

Research Triangle Park, North Carolina 

27711, telephone number (919) 541 -

5233. 

SUPPLEMENTARY INFORMATION: 

I. The Rulemaking 

Method 18 was developed for and is 

currently applicable to the speciation of 

total gaseous organics in a sample to 

determine emissions of individual 

organic compounds. In response to 

questions from industry representatives 

seeking to use the method for 

compliance demonstrations, the EPA is 

proposing to clarify the phrase 

"engineering judgment" as it relates to 

choosing a sampling and analytical 

methodology. In the proposed revision, 

an owner or operator will perform a 

laboratory evaluation of the 

methodology chosen to sample and 

analyze the compounds of interest. This 

evaluation would be used to 

characterize the effectiveness of the 

methodology and correct for any 

inefficiency in the chosen technique. 

Under subpart G of part 63, EPA is 

proposing standards to limit emissions 

of halides and halogens from 

incineration or control of halogenated 

organic vent streams at SOCMI facilities. 

Method 26 currently prescribes only 

measurement of hydrogen chloride 

emissions with sampling at a constant 

rate. The revisions being proposed today 

will expand the method's applicability 

to other hydrogen halides and halogens. 

The addition of Method 26A will 

provide an alternative to the revised 

Method 26 and will allow for isokinetic 

sampling of gas streams that are 

saturated with moisture. 

Method 26 was developed for and is 

currently applicable to determining 

hydrogen chloride emissions from 

municipal waste combustors. Methods 

similar to Method 26 and Method 26A 

were developed for the measurement pf 

hydrogen chloride (HCl) and chlorine 

(CI2) in emissions from hazardous waste 

incinerators and.boilers and industrial 

furnaces burning hazardous waste (56 

FR 32728, July 17,1991). Application of 

a method to a source with emission 

characteristics "similar" to those under 

which it was validated is addressed in 

section 12 of proposed Method 301, 

"Field Validation of Emission 

Concentrations from Stationary 

Sources" (56 FR 27370, June 13,1991). 

The Agency has compared the 

characteristics of incinerated SOCMI 

process vent gases to emissions from 

municipal waste combustors and 

hazardous waste incinerators and plans 

to waive the Method 301 validation 

requirements for applying the : 

methodology developed for waste 

incinerators to the incinerated SOCMI 

vent gases. The Agency believes that the 

sample gas matrices from incinerated 

SOCMI process vent gases are similar to 

those of waste incinerators and do not 

contain interferences that would 

warrant a validation ofthe methodology 

for measurement of HCl or (CI2) 

emissions from this source. This initial 

opinion is based, in part, on the relative 

insensitivity ofthe methodology to 

interferences expected in the SOCMI 

exhaust gas streams. 

The revisions to Method 26 as well as 

Method 26A also extend the 

applicability ofthe methodology in 

Method 26 and the HCl/fClJ methods 

developed for hazardous waste 

incinerators and boilers and industrial 

furnaces burning hazardous waste to 

measurement of hydrogen bromide 

(HBr), hydrogen fluoride (HF), and 

bromine (Br2). The applicability 

extension is based on limited data and 

the expected similar behavior of these 

compounds to HCl and (Cl2) in regard to 

sampling and analytical procedures. 
Because of its extreme reactivity, 

fluorine (FJ should not be present in 

the sample matrix and is not addressed 

by the methods. Iodine (I2) and 

hydrogen iodide (HI) are also not 

covered by the methods because few, if 

any, of tho organ les controlled by the 

SOCMI process vent incinerators will 

t

 contain the iodine ion and, additionally, 

there are no known data to support 

measurement of h and HI with this 

technique. 

The Agency intends to assess the 

methods further, prior to promulgation, 

through laboratory and field 

evaluations. A study is underway 

concerning the potential negative bias in 

Method 26A at HCl levels below 20 

ppm; specifically, the study is 

determining tho need for replacing 

certain glass components in the 

sampling train with Teflon® to reduce 

surface adsorption effects. Another 

study is planned to address sample 

stability, particularly in regard to the 

species created by hydrolysis of the 

halogens in tho alkaline solution in the 

sampling train. Finally, a laboratory and 

Held evaluation of Method 26A will be 

conducted to assess the bias and 

precision of the method for the target 

analytes. To assist in its assessment, the 

Agency solicits comments on available 

information on the proposed 

methodology. Specifically, the Agency 

solicits comments with supporting data 

to better define the compounds present 

in the gas matrices which may, for the 

hydrogen halides and halogens 

specified in the methods, (1) be 

analytical interferences, (2) interfere 

with their quantitative collection in the 

impinger solutions, or (3) affect sample 

stability. Comments should be 

addressed to the Air Docket listed in the 

ADDRESSES section. 

II. Administrative Requirements 

A. Public Hearing . 

A public hearing will be held, if 

requested, to discuss the proposed rule 

in accordance with section 307(d)(5) of 

the Clean Air Act. Persons wishing to 

make oral presentations should contact 

EPA at the address given in the 

ADDRESSES section of this preamble. 

Oral presentations will be limited to 15 

minutes each. Any member ofthe 

public may file a written statement with 

EPA before, during, or within 30 days 

after the hearing. Written statements 

should be addressed to the Air Docket 

address given in the ADDRESSES section 

of this preamble. 

A verbatim transcript of the hearing 

and written statements will be available 

for public inspection and copying 

during normal working hours at EPA's 

Air Dcckst In Washington, DC (see 

ADDRESSES section of this preamble). 

B. Docket 

The docket is an organized and 

complete file of all the information 

submitted to or otherwise considered by 

EPA in the development of this 

proposed rulemaking. The principal 

purposes ofthe docket are: (1) To allow 

interested parties to identify and locate 

documents so that they can effectively 

participate in the rulemaking process 

and (2) to serve as the record in case of 

judicial review (except for interagency 

review materials) (section 307(d)(7)(A)). 

C. Office of Management and Budget 

Review 

1. Paperwork Reduction Act. 

This rule does not contain any 

information collection requirements 

subject to OMB review under the 

Paperwork Reduction Act of 1980,44 

U.S.C. 3501 et seq. 

2. Executive Order 12291 Review. 

Under Executive Order 12291, EPA 

must judge whether a regulation is 

"major" and, therefore, subject to the 

requirement of a regulatory impact 

analysis. The proposal of these test 

methods is not major because it will hot 

have an annual effect on the economy 

of $100 million or more; it will not 

result in a major increase in costs or 

prices; and there will be no significant 

adverse effects on competition, 

employment, investment, productivity, 

innovation, or on the ability of U.S.-

based enterprises to compete with 

foreign-based enterprises in domestic or 

export markets. This rulemaking was 

submitted to the Office of Management 

and Budget (OMB) for review as 

required by Executive Order 12291. 

D. Begulatory Flexibility Act 

Compliance 

Pursuant to the provisions of 5 U.S.C 

605(b), I hereby certify that this attached 

rule, if promulgated, will not have an 

economic impact on small entities 

because no aaditional costs will be 

incurred. 

List of Subjects in 40 CFR Part 60 

Air pollution control. 

Intergovernmental relations, Reporting 

and recordkeeping requirements, and 

Synthetic organic chemical 

manufacturing. 

Dated: October 29,1992. 

William K. Reilly. 

. Administrator. 

For the reasons set out in the 

preamble, part 60, title 40 of the Code 

of Federal Regulations is proposed to be 

amended as follows: 

1. The authority citation for part 60 

continues to read as follows: 

Authority: Sees. 101. Ill, 114.116. 301. 

Clean Air Act as amended (42 U.S.C 7401. 

7411,7414,7416.7601). 

Appendix A (Amended] 

2. In appendix A, Method 18 is 

proposed to be amended by adding 

paragraph (c) to section 3 and by 

revising sections 7.4.4.1 and 7.4.4.5 and 

by adding section 7.6 to read as follows: 

Method 18—Measurement of Gaseous 

Organic Compound Emissions by Gas 

Chromatography 

3. Precision and Accuracy 

** * * *' * 

(c) Recovery. After developing an 

appropriate sampling and analytical 

system for the pollutants pf interest, 

conduct the procedure in section 7.6. 

Submit the data and results of the 

recovery procedure with the reporting of 

results under section 7.5. 

7.4.4 * * * 

7.4.4.1 Determine the recovery 

efficiency of the pollutants of interest 

according to section 7.6. 

7.4.4.2 •»'*•* 

7.4.4.3 * • • • 

7.4.4.4 * * • 

7.4.4.5 Calculations. All calculations 

can be performed according to the 

respective NIOSH method. Correct all 

sample volumes to standard 

conditions. If a sample dilution 

system has been used, multiply the 

results by the appropriate dilution 

ratio. Correct all results according to 

the procedure in section 7.6.3. 

7.6 Recovery Study. After conducting 

the presurvey and identifying all of 

the pollutants of interest, assemble (in 

the laboratory or on-site) the sampling 

and analytical system to be used in 

conducting the source test. 

7.6.1 Obtain a certified gaseous 

standard (or prepare a gaseous 

standard as described in section 6.2.1 

or 6.2.2) containing all of the 

pollutants of interest present in the 

source gas stream at the level of the 

standard (±10 percent). If complying 

with an efficiency standard 

(determining the percent efficiency of 

a control device), the concentration of 

each target pollutant in the standard 

shall be at the level of the outlet to the 

control device (±10 percent). 
Federal Register 7 Vol. 58, No. 37 / Friday, February 26, 1993 7 Corrections 11711 

P.4 

7.6.2 If an integrated bag sampling 

system is to be used at the source 

(section 7.1), follow the procedure 

specified in section 7.6.2.1. If a direct 

interface (section 7.2) or a dilution 

interface (section 7.3) sampling and 

analysis procedure is to be used at the 

source, follow the procedure in 

section 7.6.2.2. If an adsorption tube 

procedure (section 7.4) is to be used 

at the source, follow the procedure in 

section 7.6.2.3. 

7.6.2.1 Set up the sampling system 

including any conditioning system 

and one of three sampling bags 

exactly as it would be assembled at 

the source. Attach the gaseous 

standard at the inlet to the sampling 

system (i.e., the tip ofthe sampling 

probe). Sample the gaseous standard 

exactly as you would extract a sample 

from the source. Analyze the standard 

sample as the source sample would be 

analyzed. Repeat this procedure three 

times (sample and analyze three 

separate bag samples). 

7.6.2.2 Set up the on-line GC, sample 

line, and any sample conditioning 

systems exactly as they would be at 

the source (if using a dilution 

interface sampling system, set up the 

heat trace and dilution system as they 

would be at the source). Attach the 

gaseous standard at the inlet to the 

sampling system (i.e., the tip ofthe 

sampling probe). Sample the gaseous 

standard exactly as you would extract 

a sample from the gas stream of the 

source. Analyze the standard as the 

source gas would be analyzed. Repeat 

this procedure three times (sample 

and analyze three standard samples). 

7.6.2.3 Assemble the sampling system 

exactly as it would be set up at the 

source, using the same amounts and 

number of adsorption tubes as those 

to be used at the source. Attach the 

gaseous standard at the inlet to the 

sampling train (i.e., the tip of the 

sampling probe). Sample the standard 

at the flow rate and sampling times to 

be used at the source. Desorb and 

analyze the adsorbent tubes in the 

laboratory using the procedures to be 

applied to the source samples. Repeat 

this procedure three times. 

7.6.3 Calculations. The relative 

standard deviation ofthe three results 

for each pollutant of interest shall be 

£10 percent. Calculate the theoretical 

concentration for each compound 

based on standard concentration, time 

sampled (if using adsorbent tubes or 

bags), and flow rate ofthe gas. 

Calculate the measured concentration 

of each compound based on the 

analytical results. Calculate fraction 

recovered by dividing measured 

concentration by theoretical 

concentration. The average fraction 

recovered (ofthe three runs) shall be 

20.7 and £1.30 for each compound of 

interest. If average fraction recovered 

<0.7 or >1.30 for a particular 

compound, the sampling and 

analytical techniques are not 

acceptable for that compound. If the 

average fraction recovered is 20.7 and 

£1.30 for a compound, correct all of 

the results from the source test before 

submitting the data by dividing 

source concentration by the average 

fraction recovered for each 

compound. 

ft « * o ft 

3. It is proposed that Method 26 of 40 

CFR part 60, appendix A be amended by 

revising the title; by revising sections 

1.1, 1.2,1.3,1.5,1.6, 2.1.3, the first 

sentence of 2.1.4, 2.1.5, 2.2.2, the 

heading of section 3.1.2, sections 3.1.3, 

3.2.2, 3.2.3, 4.1.1, 4.2, 4.3, 4.4.2, 4.4.3, 

5.2, 7.2, 7.3, 7.4; by revising Figure 26-

1; and by adding references 4 and 5 to 

section 8 to read as follows: 

Appendix A—Test Methods 

Method 26—Determination of Hydrogen 

Halide and Halogen Emissions From 

Stationary Sources—Midget Impinger 

Method 

4 ft ft ft 

1.1 Applicability. This method is 

applicable for determining emissions 

of hydrogen halides (HX) [hydrogen 

chloride (HCl), hydrogen bromide 

(HBr), and hydrogen fluoride (HF)) 

and halogens (X2) [chlorine (Cl2) and 

bromine (BrJ] from stationary 

sources. Sources, such as those 

controlled by wet scrubbers, that emit 

acid particulate matter must be 

sampled using Method 26A. [Note: 

Mention of trade names or specific 

products does not constitute 

endorsement by the Environmental 

Protection Agency.) 

1.2 Principle. An integrated sample is 

extracted from the source and passed 

through dilute sulfuric acid and dilute 

sodium hydroxide solutions which 

collect the gaseous hydrogen halides 

and halogens, respectively. The 

hydrogen halides are solubilized in 

the acidic solution and form chloride 

(CI"), bromide (Br~), and fluoride 

(F~) ions. The halogens have a very 

low solubility in the acidic solution 

and pass through to the alkaline 

solution where they are hydrolyzed to 

form a proton (H

 + ), the halide ion, 

and the hydrohalous acid (HCIO or 

HBrO). The halide ions in the separate 

solutions are measured by ion 

chromatography (IC). 

1.3 Interferences. Volatile materials, 

such as chlorine dioxide (ClOj) and 

ammonium chloride (NH4CI), which 

produce halida ions upon dissolution 

during sampling are potential 

interferents. Interferents for the halide 

measurements are the halogen gases 

which disproportionate to a hydrogen 

halide and a hydrohalous acid upon 

dissolution in water. The use of acidic 

rather than neutral or basic solutions 

for collection of the hydrogen halides 

greatly reduces the dissolution of any 

halogens passing through this 

solution. High concentrations of 

nitrogen oxides (NO,) may produce 

sufficient nitrate (N03~) to interfere 

with measurements of very low Br~ 

levels. 

1.5 Sample Stability. The collected 

CI ~ samples can be stored for up to 

4 weeks. 

1.6 Detection Limit. The analytical 

detection limit for Cl~ is 0.1 ug/ml. 

Detection limits for the other analytes 

. should be similar. 

900 0 

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Gas N 

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Filter Holder 

Heated Glass Liner 

C5L_ 

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Empty 0.1 N H2S04 0.1 N NaOH 

Rate Meter .'%_ ** ^ 

© Sampling (Figure 1C) 

Venting (Figure, 1B) 

e Purging (Figure 1A) 

JJ=C3= 

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Pump 

Dry Gas Meter "Surge Tank 

Figure 26-1 . Sampling train. 

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3P®d©E*sJS. BLBgister /Vol. 58,. No. 37: / Friday, February 26, 1993 I Corrections 137113 

2.1.3 Sample Impingers. Four 30-ml 

midget impingers with leak-free glass 

connectors. Silicone grease may be 

used, if necessary, to prevent leakage. 

For sampling at high moisture sources 

or for sampling times greater than one 

hour, an additional midget impinger 

with a shortened stem (such that the 

gas sample doss not bubble through 

the collected condensate) should be 

used in front of the first impinger. 

2.1.4 Drying Tube or Impinger. Tube 

or impinger (Mae West or midget 

design) filled with 6- to 16-mesh 

indicating type silica gel, or 

equivalent, to dry the gas sample and 

to protect the dry gas meter and 

pump. ° ° ° 

2.1.5 Filter. A 25- or 47-mm Teflon" 

mat, PallflexR TX40H175 or 

equivalent. Locate in a glass, quartz, 

or Teflon11 filter holder with a Teflon* 

or other inert filter support inside a 

filter box heated to 121 °C (250 °F). 

When the stack gas temperature 

exceeds 210 °C (410 °F) and the HCl 

concentration is greater than 20 ppm, 

a quartz-fiber may be used. 

« o o * » 

2.2 * * * 

2.2.2 Storage Bottles. 100- or 250-ml. 

high-density polyethylene bottles 

with Teflon* screw cap liners to store 

impinger samples. 

« O O O ft 

ri ft ft ft 

3 .1 • «• » 

3.1.2 Acidic Absorbing Solution. 0.1 N 

Sulfuric Add (H12SO4). ° ° " 

3.1.3 Alkaline Absorbing Solution. 0.1 

N Sodium Hydroxide (NaOH). To 

prepare 100 ml of the alkaline 

absorbing solution for the second 

impinger pair, dissolve 0.40 g of solid 

NaOH in about 90 ml of water and 

adjust the final volume to 100 ml 

using additional water. Shake well to 

mix the solution. 

3.2 " " ° 

3.2.2 Blank Solutions. Separate blank 

solutions of the absorbing reagents 

should be prepared for analysis with 

the field samples. Dilute 30 ml of each 

absorbing solution to 100 ml with 

water in separate volumetric flasks. 

3.2.3 Halide Salt Stock Standard 

Solutions. Prepare concentrated stock 

solutions from reagent grade sodium 

chloride (Nad), sodium bromide 

(NaBr), and sodium fluoride (NaF). 

Each must be dried at 110 °C for two 

or more hours and then cooled to 

room temperature in a desiccator 

Immediately before weighing. 

Accurately weigh 2.6 to 2.7 g ofthe 

dried NaCl to within 0.2 mg, dissolve 

in water, and dilute to 1 liter. 

Calculate the exact Q" concentration 

using Equation 26-8. 

ug Cl-/ml=g of NaClxlO^S^SS/SB.^ 

Eq.26-1 

In a similar manner, accurately weigh 

and solubilize 1.2 to 1.3 g of dried 

NaBr and 2.2 to 2.3 g of NaF to make 

1-liter solutions. Use Equations 26-2 

and 26-3 to calculate the Br~ and F~ 

concentrations. 

ug Br-/ml=g of NaBrxl02,x79.904/ 

102.90 Eq. 26-2 

ug F"/ml=g of NaFxl0M8.998/41.99 

Eq. 26-3 

Alternately, solutions containing a 

nominal certified concentration of 

1000 mg/L NaCl are commercially 

available as convenient stock 

solutions from which standards can 

be made by appropriate volumetric 

dilution. Refrigerate the stock 

standard solutions and store no longer 

than one month. -

ft a * o o 

4. * ° ° 

4 j o • o 

4.1.1 Preparation of Collection Train. 

Prepare the sampling train as follows: 

Pour 15 ml ofthe acidic absorbing 

solution into each one ofthe first pair 

of impingers, and 15 ml ofthe 

alkaline absorbing solution into each 

one ofthe second pair of impingers. 

Connect the impingers in series with 

the knockout impinger first, if used, 

followed by the two impingers 

containing the acidic absorbing 

solution and the two impingers 

containing the alkaline absorbing 

solution. Place a fresh charge of silica 

gel, or equivalent, in the drying tube 

or impinger at the end ofthe impinger 

train. 

« a « o o 

4.2 Sample Recovery. Disconnect the 

impingers after sampling. 

Quantitatively transfer the contents of 

the acid impingers and the knockout 

impinger, if used, to a leak-free 

storage bottle. Add the water rinses of 

each of these impingers and 

connecting glassware to the storage 

bottle. Repeat this procedure for the 

alkaline impingers and connecting 

glassware using a separate storage 

bottle. The sample bottles should be 

sealed, shaken to mix. and labeled. 

Mark the fluid level. 

4.3 Sample Preparation for Analysis. 

Note the liquid levels in the sample 

containers end confirm on the 

analysis sheet whether or not leakage 

occurred during transport. M a 

noticeable leakage has occurred, 

either void the sample o? use 

methods, subject to the approval of 

the Administrator, to correct the final 

results. Quantitatively transfer the 

sample solutions to 200-ml 

volumetric flasks, and dilute to 200 

ml with water. 

4.4 ° ° ° 

4.4.2 Before sample analysis, establish 

a stable baseline. Next, inject a sample 

of water, and determine if any Cl\ Br, 

or P appears in the chromatogram. If 

any of these ions are present, repeat 

the load/injection procedure until 

they are no longer present Analysis of 

the acid and alkaline absorbing 

solution samples requires separate 

standard calibration curves; prepare 

each according to section 5.2. Ensure 

adequate baseline separation of the 

analytes. 

4.4.3 Between injections ofthe 

appropriate series of calibration 

standards, inject in duplicate the 

reagent blanks, quality control 

sample, and the field samples. 

Measure the areas or heights of the 

CI", Br, and F" peaks. Use the average 

response to determine the 

concentrations of the field samples 

and reagent blanks using the linear 

calibration curve. The values from 

duplicate injections should agree 

within 5 percent of their mean for the 

analysis to be valid. Dilute any 

sample and the blank with equal 

volumes of water if the concentration 

exceeds that of the highest standard. 

0 ft ' O ft ft 

5 ft o o 

5.2 Ion Chromatograph. To prepare the 

calibration standards, dilute given 

amounts (1.0 ml or greater) of the 

stock standard solutions to 

convenient volumes, using 0.1 N 

H2SO4 or 0.1 N NaOH, as appropriate. 

Prepare at least four calibration 

standards for each absorbing reagent 

containing the appropriate stock 

solutions such that they are within 

the linear range of the field samples. 

Using one of the standards in each 

series, ensure adequate baseline 

separation for the peaks of interest. 

Inject the appropriate series of 

calibration standards, starting with 

the lowest concentration standard 

first both before and after injection of 

the quality control check sample, 

reagent blanks, and field samples. 

This allows compensation for any 

instrument drift occurring during 

sample analysis. 

Determine the peak areas, or heights, 

for the standards and plot individual 

values versus halide ion concentrations 

in ug/ml. Draw a smooth curve through 

the points. Use linear regression to 

calculate a formula describing the 

resulting linear curve. 

-0000 0 

y o o ft 

7.2 Total ug HCl, HBr. or HF Per 

Sample. 
P.7 

11714 Federal Register / Vol. 58, No. 37 /Friday, February 26, 1993 / Corrections 

mHX=KV. (Sx --r-Bx -) Eq. 26-4 

where: 

Bx -= Analysis of reagent blank, ug 

halide ion (CI-, Br^, F_)/ml. 

mKx=Mass of HCl, HBr, or HF in 

sample, ug. 

Sx -= Analysis of sample, ug halide ion 

(a-.Br-.F-J/ml. 

V,=Volume of filtered and diluted 

sample, ml. 

KHo=1.028 (ug HCl/ug-mole)/(ug CI-/ 

ug-mole). 

KHBr=1.013 (ug HBr/ug-mole)/(ug Br-/ 

Ug-mole). 

K„F=1.053 (ug HF/ug-mole)/(ug F~/ugmole). 

7.3 Total ug Cl2 or Br2 Per Sample. 

mXJ=2 V. (Sx - - Bx -) Eq. 26-5 

where: 

mX2=Mass of Cl2 or Br2 in sample, ug. 

7.4 Concentration of Hydrogen Halide 

or Halogen in Flue Gas. 

C=K mHx.x2/V„s<.td) Eq. 26-6 

where: 

C=Concentration of hydrogen halide 

(HX) or halogen (X2), dry basis, mg/ 

dscm. 

Vm(Sui)'=Dry gas volume measured by 

the dry gas meter, corrected to 

standard conditions, dscm. 

K-10"3mg/ug. 

0 * * * 

4. Stern, D.A., B.M. Myatt. J.F. 

Lachowski, and K.T. McGregor. 

Speciation of Halogen and Hydrogen 

Halide Compounds in Gaseous 

Emissions. In: Incineration and 

Treatment of Hazardous Waste: 

Proceedings of the 9th Annual 

Research Symposium, Cincinnati, 

Ohio, May 2-4,1983. Publication 

No.600/9-84-015. July 1984. 

Available from National Technical 

Information Service, Springfield, VA 

22161 as PB84-234525. 

5. Holm, R.D. and S.A. Barksdale. 

Analysis of Anions in Combustion 

Products. In: Ion Chromatographic 

Analysis of Environmental Pollutants. 

E. Sawicki, J.D. Mulik, and E. 

Wittgenstein (eds.). Ann Arbor, . 

Michigan, Ann Arbor Science 

Publishers. 1978. pp. 99-110. 

o ft o a o 

4. It is proposed that 40 CFR part 60 be 

amended by adding Method 26A to 

Appendix A as follows: 

Appendix A—Test Methods 

Method 26A—-Determination of 

Hydrogen Halide and Halogen 

Emissions From Stationary Sources— 

Isokinetic Method 

1. Applicability, Principle, Interferences, 

Precision, Bias, and Stability 

1.1 Applicability. This method is 

applicable for determining emissions 

of hydrogen halides (HX) [hydrogen 

chloride (HCl), hydrogen bromide 

(HBr), and hydrogen fluoride (HF)] 

and halogens (X2) [chlorine (CI2) and 

bromine (Br2)j from stationary 

sources. This method collects the 

emission sample isokinetically and is 

therefore particularly suited for 

sampling at sources, such as those 

controlled by wet scrubbers, emitting 

acid particulate matter (e.g., hydrogen 

halides dissolved in water droplets). 

[Note: Mention of trade names or 

specific products does not constitute 

endorsement by the Environmental 

Protection Agency.) 

1.2 Principle. Gaseous and particulate 

pollutants are withdrawn 

isokinetically from the source and 

collected in an optional cyclone, on a 

filter, and in absorbing solutions. The 

cyclone collects any liquid droplets 

and is not necessary if the source 

emissions do not contain them; 

however, it is preferable to include 

the cyclone in the sampling train to 

protect the filter from any moisture 

present. The filter collects other 

particulate matter including halide 

salts. Acidic and alkaline absorbing 

solutions collect the gaseous 

hydrogen halides and halogens, 

respectively. Following sampling of 

emissions containing liquid droplets, 

any halides/halogens dissolved in the 

liquid in the cyclone and on the filter 

are vaporized to gas and collected in 

the impingers by pulling conditioned 

ambient air through the sampling 

train. The hydrogen halides are 

solubilized in the acidic solution and 

form chloride (CI~), bromide (Br"), 

and fluoride (F~) ions. The halogens 

have a very low solubility in the 

acidic solution and pass through to 

the alkaline solution where they are 

hydrolyzed to form a proton (H+), the 

halide ion, and the hypohalous acid 

(HCIO or HBrO). The halide ions in 

the separate solutions are measured 

by ion chromatography (IC). If 

desired, the particulate matter 

recovered from the filter and the 

probe is analyzed following the 

procedures in Method 5. 

1.3 Interferences. Volatile materials, 

such as chlorine dioxide (C102) and 

ammonium chloride (NH4CI), which 

produce halide ions upon dissolution 

during sampling are potential 

interferents. Interferents for the halide 

measurements are the halogen gases 

which disproportionate to a hydrogen 

halide and an hypohalous acid upon 

dissolution in water. The use of acidic 

rather than neutral or basic solutions 

for collection of the hydrogen halides 

greatly reduces the dissolution of any 

halogens passing through this 

solution. High concentrations of 

nitrogen oxides (NO,) may produce 

sufficient nitrate (NOa

 - ) to interfere 

with measurements of very low Br~ 

levels. 

1.4 Precision and Bias. The method 

has a measurable negative bias below 

20 ppm HCl. Similar bias for the other 

hydrogen halides is possible. 

1.5 Sample Stability. The collected 

CI" samples can be stored for up to 

4 weeks for analysis for HCl and Cl3. 

1.6 Detection Limit. The in-stack 

detection limit for HCl is 

approximately 0.02 ug per liter of 

stack gas; the analytical detection 

limit for HCl is 0.1 ug/ml. Detection 

limits for the other analytes should be 

similar. 

2. Apparatus 

2.1 Sampling. The sampling train is 

shown in Figure 26A-1; the apparatus 

is similar to the Method 5 train where 

noted as follows: ' 

2.1.1 Probe Nozzle. Borosilicate or 

quartz glass; constructed and 

calibrated according to Method 5, 

sections 2.1.1 and 5.1, and coupled to 

the probe liner using a Teflon® union; 

a stainless steel nut is recommended 

for this union. When the stack 

temperature exceeds 210 °C (410 °F), 

a onerpiece glass nozzle/liner 

assembly must be used. 

2.1.2 Probe Liner. Same as Method 5, 

section 2.1.2, except metal liners shall 

not be used. Water-cooling of the 

stainless steel sheath is recommended 

at temperatures exceeding 500 "C 

2.1.3 Pitot Tube, Differential Pressure 

Gauge, Filter Heating System, 

Metering System, Barometer, Gas 

Density Determination Equipment. 

Same as Method 5, sections 2.1.3, 

2.1.4, 2.1.6, 2.1.8, 2.1.9, and 2.1.10. 

2.1.4 Cyclone (Optional). Glass. Use of 

the cyclone is required only when the 

sample gas stream is saturated with 

moisture; however, the cyclone is 

recommended to protect the filler 

from any moisture droplets present. 

2.1.5 Filter Holder. Borosilicate glass, 

with a Teflon0 filter support and a 

sealing gasket. The sealing gasket 

shall be constructed of Teflon0 or 

equivalent materials. The holder 

design shall provide a positive seal 

against leakage at anypoint along the 

filter circumference. The holder shall 
P.8 

Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 11715 

be attached immediately to the outlet 

ofthe cyclone. 

2.1.6 Impinger Train. The following 

system shall be used to determine the 

stack gas moisture content and to 

collect the hydrogen halides and 

halogens: five or six impingers 

connected in series with leak-free 

ground glass fittings or any similar 

leak-free noncontaminating fittings. 

The first impinger shown in Figure 

26A-1 (knockout or condensate 

impinger) is optionel and is 

recommended as a water knockout 

trap for use under high moisture 

conditions. If used, this impinger 

should be constructed as described 

below for the alkaline impingers. but 

with a shortened stem, and should 

contain 50 ml of 0.1 N H2SO4. The 

following two impingers (acid 

Impingers which each contain 100 ml 

of 0.1 N H2S04) shall be of the 

Greenburg-Smith design with the 

standard tip (Method 5, section 2.1.7). 

The next two impingers (alkaline 

impingers which each contain 100 ml 

of 0.1 N NaOH) and the last impinger 

(containing silica gel) shall be of the 

modified Greenburg-Smith design 

(Method 5, section 2.1.7). The 

condensate, acid, and alkaline' 

impingers shall contain known 

quantities of the appropriate 

absorbing reagents. The last impinger 

shall contain a known weight of silica 

gel or equivalent desiccant. 

2.1.7 Ambient Air Conditioning Tube 

(Optional). Tube tightly packed with 

approximately 150 g of fresh 8 to 20 

mesh sodium hydroxide-coated silica, 

or equivalent; (Ascarite D® has been 

found suitable) to dry and remove 

acid gases from the ambient air used 

to remove moisture from the filter and 

cyclone, when the cyclone is used. 

The inlet and outlet ends ofthe tube 

should be packed with at least 1-cm 

thickness of glass wool or filter 

material suitable to prevent escape of 

fines. Fit one end with flexible tubing, 

etc. to allow connection to probe 

nozzle following the test run. 

2.2 Sample Recovery. The following 

items are needed: 

2.2.1 Probe-Liner and Probe-Nozzle 

Brushes, Wash Bottles, Glass Sample 

Storage Containers, Petri Dishes, 

Graduated Cylinder or Balance, and 

Rubber Policeman. Same as Method 5, 

sections 2.2.1, 2.2.2, 2.2.3, 2.2.4, 2.2.5, 

and 2.2.7. 

2.2.2 Plastic Storage Containers. 

Screw-cap polypropylene or 

polyethylene containers to store silica 

gel. High-density polyethylene bottles 

with Teflon screw cap liners to store 

impinger reagents, 1-liter. 

2.2.3 Funnels. Glass or high-density 

polyethylene, to aid in sample 

recovery. 

2.3 Analysis. For analysis, the 

following equipment is needed: 

2.3.1 Volumetric Flasks. Class A, 

various sizes. 

2.3.2 Volumetric Pipettes. Class A. 

assortment, to dilute samples to 

calibration range of the ion 

chromatograph (IC). 

2.3.3 Ion Chromatograph. Suppressed 

or nonsuppres3ed, with a 

conductivity detector and electronic 

integrator operating in the peak area 

mode. Other detectors, a strip chart 

recorder, and peak heights may be 

used. 

3. Beagenis 

Unless otherwise indicated, all reagents 

must conform to the specifications of 

the Committee on Analytical Reagents 

of the American Chemical Society 

(ACS reagent grade). When such 

specifications are not available, the 

best available grade shall be used. 

3.1 Sampling. 

3.1.1 Water. Deionized, distilled water 

that conforms to American Society of 

Testing and Materials (ASTM) 

Specification D1193-77, Typo 3. 

3.1.2 Acidic Absorbing Solution, 0,1 N 

Sulfuric Acid (H2Sb,i}. To prepare 1 L, 

slowly add 2.80 ml of concentrated 

H2S04 to about 900 ml of water while 

stirring, and adjust the final volume to 

1 L using additional water. Shake well 

to mix the solution. 

3.1.3 Alkaline Absorbing Solution. 0.1 

N Sodium Hydroxide (NaOH). To 

prepare 1 L, dissolve 4.00 g of solid 

NaOH in about 900 ml of water and 

adjust the final volume to 1 L using 

additional water. Shake well to mix 

the solution. 

3.1.4 Filter. Quartz-fiber or Teflon® 

mat (e.g., Pallflex® TX40HI45) filter. 

3.1.5 Silica Gel, Crushed Ice, and 

Stopcock Grease. Same as Method 5, 

sections 3.1.2, 3.1.4, and 3.1.5, 

respectively. 

3.2 Sample Recovery. 

3.2.1 Water. Same as Section 3.1.1. 

3.2.2 Acetone. Same as Method 5, 

Section 3.2. 

3.3 Sample Analysis. 

3.3.1 Water. Same as section 3.1.1. 

3.3.2 Reagent Blanks. A separate blank 

solution of each absorbing reagent 

should be prepared for analysis with 

the field samples. Dilute 200 ml of 

each absorbing solution (250 ml ofthe 

acidic absorbing solution, if a 

condensate impinger is used) to the 

same final volume as the field 

samples using the blank sample of 

rinse water. If a particulate 

determination is conducted, collect a 

blank sample of acetone. 

3.3.3 Halide Salt Stock Standard 

Solutions. Prepare concentrated stock 

solutions from reagent grade sodium 

chloride (NaCl), sodium bromide 

(NaBr). and sodium fluoride (NaF). 

Each must be dried at 110 °C for 2 or 

more hours and then cooled to room 

temperature in a desiccator 

immediately before weighing. 

Accurately weigh 1.6 to 1.7 g of the 

dried NaCl to within 0.1 mg, dissolve 

in water, and dilute to 1 liter. 

Calculate the exact Cl~ concentration 

using Equation 26 A-1. 

ug Cl_/ml=g of NaClxl03x35.453/58.44 

Eq. 26A-1 

In a similar manner, accurately weigh 

and solubilize 1.2 to 1.3 g of dried 

NaBr and 2.2 to 2.3 g of NaF to make 

1-liter solutions. Use Equations 26A2 and 26A-3 to calculate the Br~ and 

F ~ concentrations. 

ug Br_/ml=g of NaBrxlO,x79.904/ 

102.90 Eq. 26A-2 

ug F-/ml=g olr1aFxWbilB.998hl.Q9 

Eq. 26A-3 

Alternately, solutions containing a 

nominal certified concentration of 

1000 mg/L NaCl are commercially 

available as convenient stock 

solutions from which standards can 

be made by appropriate volumetric 

dilution. Refrigerate the stock 

standard solutions and store no longer 

than 1 month. 

3.3.4 Chromatographic Eluent. 

Effective eluents for nonsuppressed 

ion chromatography using a resin- or 

silica-based weak ion exchange 

column are a 4 mM potassium 

hydrogen phthalate solution, adjusted 

to a pH of 4.0 using a saturated 

sodium borate solution, and a mM 4-

hydroxy benzoate solution, adjusted 

to a pH of 8.6 using 1 N sodium 

hydroxide. An effective eluent for 

suppressed ion chromatography is a 

solution containing 3 mM sodium 

bicarbonate and 2.4 mM sodium 

carbonate. Other dilute solutions 

buffered to a similar pH that contain 

no ions interfering with the 

chromatographic analysis may be 

used. If, when using suppressed ion 

chromatography, the "water dip" 

resulting from sample injection is 

interfering with the chlorine peak, use 

a 2 mM sodium hydroxide/2.4 mM 

sodium bicarbonate eluent. 

4. Procedure 

Because ofthe complexity of this 

method, testers and analysts should 

be trained and experienced with the 

procedures to ensure reliable results4.1 Sampling. 

4.1.1 Pretest Preparation. Follow the 

general procedure given in Method 5. 
P.9 

11716 Federal Register / Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

section 4,1.1, except the filter need 

only be desiccated and weighed if a 

particulate determination will be 

conducted. 

4.1.2 Preliminary Determinations. 

Same as Method 5, section 4.1.2. 

4.1.3 Preparation of Sampling Train; 

Follow the general procedure given in 

Method 5, section 4.1.3, except for the 

following variations: 

Add 50 ml of 0.1 N H2S04 to the 

condensate impinger, if used. Place 

100 ml of 0.1 N H2S04 in each of the 

next two impingers. Place 100 ml of 

0.1 N NaOH in each of the following 

two impingers. Finally, transfer 

approximately 200-300 g of 

preweighed silica gel from its 

container to the last impinger. Set up 

the train as in Figure 26A-1. When 

used, the optional cyclone is inserted 

between the probe liner and filter 

holder and located in the heated filter 

box. . . 

4.1.4 Leak-Check Procedures. Follow 

the leak-check procedures given in 

Method 5, sections 4.4.1 (Pretest LeakChock), 4.1.4.2 (Leak-Checks During 

the Sample Run), and 4.1.4.3 (PostTest Leak-Check); 

4.1.5 Train Operation. Follow the 

general procedure given in Method 5, 

section 4.1.5. Maintain a temperature 

around the filter and (cyclone, if used) 

of 120+14 °C (248125 °F). For each 

run, record the data required on a data 

sheet such as the one shown in 

Method 5, Figure 5-2. If the 

condensate impinger becomes too 

full, it maybe emptied, recharged 

with 50 ml of 0.1 N H2S04, and 

replaced during the sample run. The 

condensate emptied must be saved 

and included in the measurement of 

the volume of moisture collected and 

included in the sample for analysis. 

The additional 50 ml of absorbing 

reagent must also be considered in 

calculating the moisture. After the 

impinger is reinstalled in the train, 

conduct a leak-check as described in 

Method 5, section 4.1.4.2. 

4.1.6 Post-Test Moisture Removal 

(Optional). When a cyclone is 

included in the sampling train, 

perform the following procedure. 

Upon completion of the test run, 

connect the ambient air conditioning 

tube at the probe inlet and operate the 

train with the filter heating system at 

120±14 °C (248±25 °F) at a low flow 

rate (e.g., AH=1 in. H20) to vaporize 

any liquid and hydrogen halides in 

the cyclone or on the filter and pull 

them through the train into the 

impingers. After 30 minutes, turn off 

the flow, remove the conditioning 

tube, and examine the cyclone and 

filter for any visible moisture. If 

moisture is visible, repeat this step for 

15 minutes. 

4.2 Sample Recovery.: Allow the probe 

to cool. When the probe can be 

handled safely > wipe off all the 

external.surfaces of the tip of the 

probe nozzle and place a cap loosely 

over the tip. Do not cap the probe tip 

tightly while the sampling train is 

cooling down because this will create 

a vacuum in the filter holder, drawing 

water from the impingers into the 

holder. Before moving the sampling 

train to the cleanup site, remove the 

probe, wipe off any silicone grease, 

and cap the open outlet ofthe 

impinger train, being careful not to 

lose any condensate that might be 

present. Wipe off any silicone grease 

and cap the filter or cyclone inlet. 

Remove the umbilical cord from the 

last impinger and cap the impinger. If 

a flexible line is used between the 

first impinger and the filter holder, 

disconnect it at the filter holder and 

let any condensed water drain into 

the first impinger. Wipe off any 

silicone grease and cap the filter 

holder outlet and the impinger inlet. 

Ground glass stoppers, plastic caps, 

serum caps, Teflon" tape, Parafilm", 

or aluminum foil may be used to close 

these openings. Transfer the probe 

and filter/impinger assombly to the 

cleanup area. This ares should be 

clean and protected from the weather 

to minimize sample contamination or 

loss. Inspect the train prior to and 

during disassembly and note any 

abnormal-conditions. Treat samples as 

follows: 

4.2il Container No. 1 (Optional; Filter 

Catch for Particulate Determination). 

Same as Method 5, section 4.2, 

Container No. 1. 

4.2.2 Container No. 2 (Optional; FrontHalf Rinse for Particulate 

Determination). Same as Method 5, 

section 4.2, Container No. 2. 

4.2.3 Container No. 3,(Knockout and 

Acid Impinger Catch for Moisture and 

Hydrogen Halide Determination). 

Disconnect the impingers. Measure 

the liquid in the acid and knockout 

impingers to ±1 ml by using a 

graduated cylinder or by weighing it 

to ±0.5 g by using a balance. Record 

the volume or weight of liquid 

present. This information is required 

to calculate the moisture content of 

the effluent gas. Quantitatively 

transfer this liquid to a leak-free 

sample storage container. Rinse these 

impingers and connecting glassware 

(and tubing, if used) with water and 

add these rinses to the storage 

container. Seal the container, shake to 

mix, and label. The fluid level should 

be marked so that if any sample is lost 

during transport, a correction 

proportional to the lost volume can be 

applied. Retain rinse water and acidic 

absorbing solution blanks and. analyze 

with the samples.. 

4.2.4 Container No. 4; (Alkaline 

Impinger Catch for Halogen and 

Moisture Determination). Measure 

and record the liquid in the alkaline 

impingers as described in section 

4.2.3. Quantitatively transfer this 

liquid to a leak-free sample storage 

container. Rinse these two impingers. 

and connecting glassware with water 

and add these rinses to the container. 

Seal the container, shake to mix, and 

label; mark the fluid level. Retain, 

alkaline absorbing solution blank and 

analyze with the samples. 

4.2.5 Container No. 5 (Silica Gel for 

Moisture Determination). Same as 

Method 5, section 4.2, Container No. 

3. 

4.2.6 Container Nos. 6 through 9 

(Reagent Blanks): Save portions of the 

absorbing reagents (0.1 N H2S04 and 

0.1 N NaOH) equivalent to the amount 

•" used in the sampling train; dilute to 

the approximate volume of the 

corresponding samples using rinse 

water directly from the wash bottle 

being used. Also, save a portion of the 

rinse water alone and a portion of the 

acetone equivalent to the amount 

used to rinse the front half of the 

sampling train. Place each in a 

separate, prelabeled sample container. 

4.2.7 Prior to shipment, recheck all 

sample containers to ensure that the 

caps are well-secured. Seal the lids of 

all containers around the 

circumference with Teflon* tape. Ship 

all liquid samples upright and all 

particulate filters with the particulate 

catch facing upward. 

4.3 Sample Preparation and Analysis. 

Note the liquid levels in the sample 

containers and confirm on the 

analysis sheet whether or not leakage 

occurred during transport. If a 

noticeable leakage has occurred, 

either void the sample or use 

methods, subject to the approval of 

the Administrator, to correct the final 

results. 

4.3.1 Container Nos. 1 and 2 and 

Acetone Blank (Optional; Particulate 

Determination). Same as Method 5, 

section 4.3. 

4.3.2 Container No. 5. Same as Method 

5, section 4.3 for silica gel. . 

4.3.3 Container Nos. 3 and 4 and 

Absorbing Solution and Water Blanks. 

Quantitatively transfer each sample to 

a volumetric flask or graduated 

cylinder and dilute with water to a 

final volume within 50 ml of the 

largest sample.. , 
P.10 

Federal Register 7 Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 11717 

4.3.3.1 The IC conditions will depend 

upon analytical column type and 

whether suppressed or nonsuppressed 

IC is used. Prior to calibration and 

sample analysis, establish a stable 

baseline. Next, inject a sample of 

water, and determine if any Cl~. Br~. 

or F~ appears in the chromatogram. If 

any of these ions are present, repeat 

the load/injection procedure until 

they are no longer present. Analysis of 

the acid and alkaline absorbing 

solution samples requires separate 

standard calibration curves; prepare 

each according to section 5.2. Ensure 

adequate baseline separation of the 

analytes. 

4.3.3.2 Between injections of the 

appropriate series of calibration 

standards, inject in duplicate the 

reagent blanks and the field samples. 

Measure the areas or heights of the 

CI", Br~andF~ peaks. Use the 

average response to determine the 

concentrations of the field samples 

and reagent blanks using the linear 

calibration curve. If the values from 

duplicate injections are not within 5 

percent of their mean, the duplicate 

injection shall be repeated and all 

four values used to determine the 

average response. Dilute any sample 

and the blank with equal volumes of 

ivater if the concentration exceeds 

that of the highest standard. 

4.4 Audit Sample Analysis. Audit 

samples must be analyzed subject to 

availability. 

5. Calibration 

Maintain a laboratory log of ail 

calibrations. 

5.1 Probe Nozzle, Pitot Tube, Dry Gas 

Metering System, Probe Heater, 

Temperature Gauges. Leak-Check of 

Metering System, and Barometer. 

Same as Method 5. sections 5.1. 5.2. 

5.3. 5.4. 5 5, 5.6. and 5.7, respectively. 

5.2 Ion Chromatograph. To prepare the 

calibration standards, dilute given 

amounts (1.0 ml or greater) ofthe 

stock standard solutions to 

convenient volumes, using 0.1 N 

H2S04 or 0.1 N NaOH, as appropriate. 

Prepare at least four calibration 

standards for each absorbing reagent 

containing the three stock solutions 

such that they are within the linear 

range ofthe field samples. Using one 

of the standards in each series, ensure 

adequate baseline separation for the 

peaks of interest. Inject the 

appropriate series of calibration 

standards, starting with the lowest 

concentration standard first both 

before arid after injection ofthe 

quality control check sample, reagent 

blanks, and field samples. This allows 

compensation for any instrument drift 

occurring during sample analysis. 

Determine the peak areas, or height, of 

the standards and plot individual 

values versus halide ion 

concentrations in Ug/ml. Draw a 

smooth curve through the points. Use 

linear regression to calculate a 

formula describing the resulting linear 

curve. 

6. Quality Control 

Same as Method 5. Section 4.4. 

7. Quality Assurance 

7.1 Applicability. When the method is 

used to demonstrate compliance with 

a regulation, a set of two audit 

samples shall be analyzed. 

7.2 Audit Procedure. The available 

audit samples are chloride solutions. 

Concurrently analyze the two audit 

samples and a set of compliance 

samples in the same manner to 

evaluate the technique ofthe analyst 

and the standards preparation. The 

same analyst, analytical reagents, and 

analytical system shall be used both 

for compliance samples and the 

Environmental Protection Agency 

(EPA) audit samples. 

7.3 Audit Sample Availability. Audit 

samples will be supplied only to 

enforcement agencies for compliance 

tests. Audit samples may be obtained 

by writing the Sourcs Test Audit 

Coordinator (MD-77B), Quality 

Assurance Division, Atmospheric 

Research and Exposure Assessment 

Laboratory, U.S. Environmental 

Protection Laboratory, Research 

Triangle Park, NC 27711 or by calling 

the Source Test Audit Coordinator 

(STAC) at (919) 541-7834. The 

request for the audit samples should 

be made at least 30 days prior to the 

scheduled compliance sample 

analysis. 

7.4 Audit Results. Calculate the 

concentrations in mg/dscm using the 

specified sample volume in the audit 

instructions. Include the results of 

both audit samples, their 

identification numbers, and the 

analyst's name with the results of the 

compliance determination samples in 

appropriate reports to the EPA 

regional office or the appropriate 

enforcement agency. (NOTE: 

Acceptability of results may be 

obtained immediately by reporting the 

audit results in mg/dscm and 

compliance results in total ug HCl/ 

sample to the responsible 

enforcement agency.) The 

concentrations of the audit samples , 

obtained by the analyst shall agree 

within 10 percent of the actual 

concentrations. If the 10 percent 

specification is not met. reanalyze the 

compliance samples and audit 

samples, and include initial and 

reanalysis values in the test report. 

Failure to meet the 10 percent 

specification may require retests until 

the audit problems are resolved. 

8. Calculations 

Retain at least one extra decimal figure 

beyond those contained in the 

available data in intermediate 

calculations, and round off only the 

final answer appropriately. 

8.1 Nomenclature. Seme as Method 5, 

section 6.1. tn addition: 

B,-=Analysis of reagent blank, ug halide 

ion0(Cl-.Br-.F-)/ml. 

C=Concentration of hydrogen halide 

(HX) or halogen (X2), dry basis, mg/ 

dscm. 

mnx=Mass of HCl. HBr, or HF in 

sample, ug. 

mX2=Mass of C12 or Br2 in sample, ug. 

Sx-=Analysis of sample, ug halide ion 

(Cl-,Br-.F-)/ml. 

Vs=Volume of filtered and diluted 

sample, ml. 

8.2 Average Dry Gas Meter 

Temperature and Average Orifice 

Pressure Drop, See data sheet (Figure 

5-2 of Method 5). 

8.3 Dry Gas Volume. Calculate Vm<uj) 

and adjust for leakage, if necessary, 

using the equation in section S.3 of 

Method 5. 

8.4 Volume of Water Vapor and 

Moisture Content. Calculate the 

volume of water vapor y»(jUi) and 

moisture content B„, from the data 

obtained in this method (Figure 5-2 of 

Method 5); use Equations 5-2 and 5 -

3 of Method 5. 

8.5 Isokinetic Variation and 

Acceptable Results. Use Method 5. 

sections 6.11 and 6.12. 

8.6 Acetone Blank Concentration. 

Acetone Wash Blank Residue Weight. 

Particulate Weight, and Particulate 

Concentration. For particulate 

determination. 

8.7 Total ug HCl. HBr, or HF Per 

Sample. 

mHX=K V, (Sx~ -B x - j Eq. 26A-4 

where: 

KHC=1,028 (ug HCl/ug-mole)/(ug CI•"/ 

ug-mole). 

KHB,=1.013 (ug HBr/ug-mole)/(ug Br-/ 

ug-mole). 

K«F=1.0S3 (ug HF/ug-mole)/(ug F~/ugmole). 

8.8 Total ug Cl2 or Br2 Per Sample. 

mx2=2VI (Sx --Bx-) Eq.26A-5 

8.9 Concentration of Hydrogen Halide 

or Halogen in Flue Gas. 

4C=K mMxJCi/Vvnfstd) Eq. 26A-6 

where: 

K=10~3 mg/ug 
P.11 

11718 Federal Register 7 Vol. 58, No. 37 / Friday, February 26, 1993 / Corrections 

8.10 Stack Gas Velocity and 

Volumetric Flow Rata Calculate the 

average stack gas velocity and 

volumetric flow rate, if needed, using 

data obtained in this method and the 

equations in sections 5.2 and 5.3 of 

Method 2. 

9. Bibliography 

1. Steinsberger, S.C and J.H. Margeson. 

Laboratory and Field Evaluation of a 

Methodology for Determination of 

Hydrogen Chloride Emissions from 

Municipal and Hazardous Waste 

Incinerators. U.S. Environmental 

Protection Agency, Office of Research 

and Development. Publication No. 

600/3-89/064. April 1989. Available; 

from National Technical Information 

Service, Springfield, VA 22161 as 

PB89220586/AS. 

. State of California Air Resources 

Board. Method 421—Determination of 

Hydrochloric Acid Emissions from 

Stationary Sources. March 18,1987. 

. Cheney, J.L. and CR. Fortune. 

Improvements in the Methodology for 

Measuring Hydrochloric Acid in 

Combustion Source Emissions. J. 

Environ. Scii Health. A19{3): 337-350. 

1984. 

. Stern, D.A., B.M. Myatt, J.F. 

Lachowski, and K.T. McGregor. 

Spociation of Halogen and Hydrogen 

Halide Compounds in Gaseous 

Emissions. In: Incineration and . 

Treatment of Hazardous Waste: 

Proceedings ofthe 9th Annual 

Research Symposium, Cincinnati, 

Ohio, May 2-4,1983. Publication No. 

600/9-84-015. July 1984. Available 

from National Technical Information 

Service, Springfield, VA 22161 as 

PB84-234525. 

5. Holm, R.D. and S.A. Barksdale. 

Analysis of Anions in Combustion 

Products. In: Ion Chromatographic 

Analysis of Environmental Pollutants, 

E. Sawicki, J.D. Mulik, and E. 

Wittgenstein (eds.)J. Ann Arbor, 

Michigan; Ann Arbor Science 

Publishers. 1978. pp. 99-110. 

BILLING COSE 150541-0 • 
Teflon or Quartz 

Filter 

Heated 

" Box 

Pilot Tube 

Thermometer 

Manometer 

Silica" Gel 

0.1N NaOH 

0.1N H2S04 

•Calibrator! 

Orifice 

Coars< 

Fi 

• 

coarse-, 

\ vacuum 

neX 1 ®u 9 e 

Inclined Dry Gas Vacuum 

Manometer Meter Pump 

% 

• » 

EL 

a 

< 

en 

05 

Z 

p 

3. 

o. 

v: 

cr 

3 

CO 

co 

Figure 26A-1. Sampling train 

BILUNO CODE 150M1-C 

BILUNO CODE 1506-01-0 

O 

S3 

CA 

ce