P.1 

OAR Box 1878 

Prepped by Charmelle Mathews 

Document Number: 

87) 11-1-17 

Docket Number: 

A-90-19 

Printed 11/28/20081:21:24 PM Sheet 87 of 145 
§60.660 

(e) With every fresh stock of starch 

solution perform a blank test as follows: Introduce fresh starch solution 

Into burette up to 100 ml mark. Close 

(P) and (O). Lower (L) and open (O). 

When liquid level reaches the 10 ml 

mark, close (O). With air ln burette, titrate as during a test and up to same 

end point. Call ml of iodine used C. 

Then, 

Grains H,S per 100 cubic foot of gas =100 

(D-C) 

(f) Greater sensitivity can be attained If a 500 ml capacity Tutwiler 

burette is used with a more dilute 

(0.001N) Iodine solution. Concentrations less than 1.0 grains per 100 cubic 

foot can be determined in this way. 

Usually, the starch-iodine end point Is 

much less distinct, and a blank determination of end point, with H»S-free 

gas or air, is required. 

Figure I, Tutweer burette (lettered Heme mentioned 

in text) 

40 CFR Ch. I (7-1-9 1 Edition) 

Subpart MM M [ReservedJ 

Subpart NNN—Standard s of Parformanco for Volatile Organic Compound (VOC ) Emissions From 

Synthetic Organic Chomical Man -

ufacturing Industry (SOCMI ) Distillation Operations 

SOURCE: 55 FR 26942. June 29. 1990, unless 

otherwise noted. 

§60.660 Applicability and designation of 

affected facility. 

(a) The provisions of this subpart 

apply to each affected facility designated in paragraph (b) of this section 

that is part of a process unit that produces any of the chemicals listed In 

8 60.667 as a product, co-product, byproduct, or intermediate, except as 

provided ln paragraph (c). 

(b) The affected facility is any of the 

following for which construction, 

modification, or reconstruction commenced after December 30. 1983: 

(1) Each distillation unit not discharging its vent stream Into a recovery system. 

(2) Each combination of a distillation unit and the recovery system Into 

which its vent stream is discharged. 

(3) Each combination of two or more 

distillation units and the common recovery system into which their vent 

streams are discharged. 

(c) Exemptions from the provisions 

of paragraph (a) of this section are as 

follows: 

(1) Any distillation unit operating as 

part ot a process unit which produces 

coal tar or beverage alcohols, or which 

uses, contains, and produces no VOC is 

not an affected facility. 

(2) Any distillation unit that is subject to the provisions of Subpart DDD 

is not an affected facility. 

(3) Any distillation unit that is designed and operated as a batch operation Is not an affected facility. 

(4) Each affected facility that has a 

total resource effectiveness (TRE) 

index value greater than 8.0 is exempt 

from all provisions of this subpart 

except for SS 60.662: 60.664 (d). (e), 

and (f); and 60.665 (h) and (1). 

(5) Each affected facility in a process unit with a total design capacity 

616 

Environmental Protection Agency 

for all chemicals produced within that 

unit of less than one glgagram per 

year Is exempt from all provisions of 

this subpart except for the recordkeeping and reporting requirements In 

paragraphs (j), <1)(6). and (n) of 

i 60.665. 

(6) Each affected facility operated 

with a vent stream flow rate less than 

0.008 scm/mln Is exempt from all provisions of this subpart except for the 

test method and procedure and the 

recordkeeping and reporting requirements in S 60.664(g) and paragraphs 

(I). (1X5), and (o) of S 60.665. 

[Non: The intent of these standards is to 

minimize the emissions of VOC through the 

application of best demonstrated technology (BDT). The numerical emission limits In 

these standards are expressed ln terms of 

total organic compounds (TOC). measured 

as TOC less methane and ethane. This emission limit reflects the performance of BDT.] 

§ 60.661 Definitions. 

As used in this subpart, all terms not 

defined here shall have the meaning 

given them in the Act and in subpart 

A of part 60, and the following terms 

shall have the specific meanings given 

them. 

Batch distillation operation means a 

noncontiguous distillation operation 

in which a discrete quantity or batch 

of liquid feed Is charged Into a distillation unit and distilled at one time. 

After the initial charging of the liquid 

feed, no additional liquid is added 

during the distillation operation. 

Boiler means any enclosed combustion device that extracts useful energy 

ln the form of steam. 

By compound means by Individual 

stream components. not carbon 

equivalents. 

Continuous recorder means a data 

recording device recording an instantaneous data value at least once every 15 

minutes. 

Distillation operation means an operation separating one or more feed 

stream(s) into two or more exit 

stream*s). each exit stream having 

component concentrations different 

from those in the feed stream(s). The 

separation is achieved by the redistribution of the components between the 

liquid and vapor-phase as they ap-

§60.661 

proach equilibrium within the distillation unit. 

Distillation unit means a device or 

vessel in which distillation operations 

occur, including all associated internals (such as trays or packing) and accessories (such as reboiler. condenser, 

vacuum pump, steam Jet, etc.), plus 

any associated recovery system. 

Flame zone means the portion of the 

combustion chamber in a boiler occupied by the flame envelope. 

Flow indicator means a device which 

indicates whether gas flow is present 

in a vent stream. 

Halogenated vent stream means any 

vent stream determined to have a total 

concentration (by volume) of compounds containing halogens of 20 

ppmv (by compound) or greater. 

Incinerator means any enclosed 

combustion device that is used for destroying organic compounds and does 

not extract energy ln the form of 

steam or process heat. 

Process theater means a device that 

transfers heat liberated by burning 

fuel to fluids contained in tubes, including all fluids except water that is 

heated to produce steam. 

Process unit means equipment assembled and connected by pipes or 

ducts to produce, as intermediates or 

final products, one IT more of the 

chemicals in 5 60.667. A process unit 

can operate Independently If supplied 

with sufficient fuel or raw materials 

and sufficient product storage facilities. 

Product means any compound or 

chemical listed ln S 60.667 that Is produced for sale as a final product as 

that chemical, or for use in the production of other chemicals or compounds. By-products, co-products, and 

intermediates are considered to be 

products. 

Recovery device means an individual 

unit of equipment, such as an absorber, carbon adsorber, or condenser, capable of and used for the purpose of 

recovering chemicals for use. reuse"," or 

sale. 

Recovery system means an Individual 

recovery device or series of such •devices applied to the same vent stream. 

TofaZ organic compounds (TOC) 

means those compounds measured* according to the procedures \ in 

% 

ij 

7= > 

T " l 

-* CD 

CO 

617 

TJ 
§60.662 

8 60.664(b)(4). For the purposes of 

measuring molar composition as required in 5 60.664(d)(2)(i): hourly emissions rate as required in 5 60.664(d)(5) 

and i 60.664(e); and TOC concentration as required in J 60.665(b)(4) and 

i 60.665(g)(4). those compounds which 

the Administrator has determined do 

not contribute appreciably to the formation of ozone are to be excluded. 

The compounds to be excluded are 

identified in Environmental Protection Agency's statements on ozone 

abatement policy for State Implementation Plans (SIP) revisions (42 FR 

35314; 44 FR 32042; 45 FR 32424; 45 

FR 48942). 

TRE index value means a measure of 

the supplemental total resource requirement per unit reduction of TOC 

associated with an individual distillation vent stream, based on vent stream 

flow rate, emission rate of TOC net 

heating value, and corrosion properties (whether or not the vent stream is 

halogenated), as quantified by the 

equation given under . 60.664(e). 

Vent stream means any gas stream 

discharged directly from a distillation 

facility to the atmosphere or indirectly to the atmosphere after diversion 

through other process equipment. The 

vent stream excludes relief valve discharges and equipment leaks including, but not limited to, pumps, compressors, and valves. 

§ 60.662 Standards. 

Each owner or operator of any affected facility shall comply with paragraph (a), (b), or (c) of this section for 

each vent stream on and after the date 

on which the Initial performance test 

required by . 60.8 and § 60.664 is completed, but not later than 60 days after 

achieving the maximum production 

rate at which the affected facility will 

be operated, or 180 days after the initial start-up, whichever date comes 

first. Each owner or operator shall 

either: 

(a) Reduce emissions of TOC (less 

methane and ethane) by 98 weightpercent, or to a TOC (less methane 

and ethane) concentration of 20 ppmv, 

on a dry basis corrected to 3 percent 

oxygen, whichever is less stringent. If 

a boiler or process heater is used to 

comply with this paragraph, then the 

40 CFR Ch. I (7-1-91 Edition) 

vent stream shall be introduced into 

the flame zone of the boiler or process 

heater; or 

(b) Combust the emissions in a flare 

that meets the requirements of 

5 60.18; or 

(c) Maintain a TRE index value 

greater than 1.0 without use of VOC 

emission control devices. 

§ 60.663 Monitoring of emissions and operations. 

(a) The owner or operator of an affected facility that uses an Incinerator 

to seek to comply with the TOC emission limit specified under 5 60.662(a) 

shall install, calibrate, maintain, and 

operate according to manufacturer's 

specifications the following equipment: 

( D A temperature monitoring device 

equipped with a continuous recorder 

and having an accuracy of ±1 percent 

of the temperature being monitored 

expressed in degrees Celsius or ±0.5 

*C, whichever Is greater. 

(1) Where an incinerator other than 

a catalytic incinerator is used, a temperature monitoring device shall be installed in the firebox. 

" (11) Where a catalytic incinerator is 

used, temperature monitoring devices 

shall be installed in the gas stream immediately before and after the catalyst bed. 

(2) A flow indicator that provides a 

record of vent stream flow to the incinerator at least once every hour for 

each affected facility. The flow indicator shall be installed in the vent 

stream from each affected facility at a 

point closest to the inlet of each incinerator and before being Joined with 

any other vent stream. 

(b) The owner or operator of an affected facility that uses a flare to seek 

to comply with {60.662(b) shall install, calibrate, maintain and operate 

according to manufacturer's specifications the following equipment: 

( D A heat sensing device, such as a 

ultra-violet beam sensor or thermocouple, at the pilot light to indicate the 

continuous presence of a flame. 

(2) A flow indicator that provides a 

record of vent stream flow to the flare 

at least once every hour for each affected facility. The flow Indicator 

618 

Environmental Protection Agency 

shall be Installed in the vent stream 

from each affected facility at a point 

closest to the flare and before being 

joined with any other vent stream. 

(c) The owner or operator of an affected facility that uses a boiler or 

process heater to seek to comply with 

{60.662(a) shall Install, calibrate, 

maintain and operate according to the 

manufacturer's specifications in the 

following equipment: 

( D A flow indicator that provides a 

record of vent stream flow to the 

boiler or process heater at least once 

every hour for each affected facility. 

The flow indicator shall be Installed in 

the vent stream from each distillation 

unit within an affected facility at a 

point closest to the inlet of each boiler 

or process heater and before being 

joined with any other vent stream. 

(2) A temperature monitoring device 

in the firebox equipped with a continuous recorder and having an accuracy 

of ±1 percent of the temperature 

being measured expressed in degrees 

Celsius or ±0.5 °C, whichever is greater, for boilers or process heaters of less 

than 44 MW (150 million Btu/hr) heat 

input design capacity. 

(3) Monitor and record the periods 

of operation of the boiler or process 

heater lf the design heat input capacity of the boiler or process heater is 44 

MW (150 million Btu/hr) or greater. 

The records must be readily available 

for Inspection. 

(d) The owner or operator of an affected facility that seeks to comply 

with the TRE index value limit specified under S 60.662(c) shall Install, calibrate, maintain, and operate according 

to manufacturer's specifications the 

following equipment, unless alternative monitoring procedures or requirements are approved for that facility by 

the Administrator: 

(D Where an absorber is the final recovery device in the recovery system: 

(i) A scrubbing liquid temperature 

monitoring device having an accuracy 

of ±1 percent of the temperature 

being monitored expressed in degrees 

Celsius or ±0.5 "C, whichever is greater, and a specific gravity monitoring 

device having an accuracy of ±0.02 

specific gravity units, each equipped 

with a continuous recorder, or 

§60.663 

(ii) An organic monitoring device 

used to indicate the concentration 

level of organic compounds exiting the 

recovery device based on a detection 

principle such as infrared, photoionizatlon, or thermal conductivity, each 

equipped with a continuous recorder. 

(2) Where a condenser is the final 

recovery device in the recovery 

system: 

(i) A condenser exit (product side) 

temperature monitoring device 

equipped with a continuous recorder 

and having an accuracy of ± 1 percent 

of the temperature being monitored 

expressed In degrees Celsius or ±0.5 

°C, whichever is greater, or 

(ii) An organic monitoring device 

used to monitor organic compounds 

exiting the recovery device based on a 

detection principle such as Infra-red, 

photoionization, or thermal conductivity, each equipped with a continuous 

recorder. 

(3) Where a carbon adsorber is the 

final recovery device unit in the recovery system: 

(1) An integrating steam flow monitoring device having an accuracy of 

±10 percent, and a carbon bed temperature monitoring device having an accuracy of ±1 percent of the temperature being monitored expressed in degrees Celsius or ±0.5 °C, whichever is 

greater, both equipped with a continuous recorder, or 

(ii) An organic monitoring device 

used to indicate the concentration 

level of organic compounds exiting the 

recovery device based on a detection 

principle such as infra-red, photoionization, or thermal conductivity, each 

equipped with a continuous recorder. 

(e) An owner or operator of an affected facility seeking to demonstrate 

compliance with the standards specified under 5 60.662 with control devices other than incinerator, boiler, 

process heater, or flare; or recovery 

device other than an absorber, condenser, or carbon absorber shall provide to the Administrator information 

describing the operation of the control 

device or recovery device and the process parameters) which would indicate 

proper operation and maintenance of 

the device. The Administrator may request further information and will 

•3. 

2* 

fl 

619 
§60.664 

specify appropriate monitoring procedures or requirements. 

§ 60.664 Test methods and procedures. 

(a) For the purpose of demonstrating compliance with { 60.662, all affected facilities shall be run at full operating conditions and flow rates 

during any performance test. 

(b) The following methods ln appendix A to this part, except as provided 

under 5 60.8(b), shall be used as reference methods to determine compliance 

with the emission limit or percent reduction efficiency specified under 

9 60.662(a). 

(1) Method 1 or IA, as appropriate, 

for selection of the sampling sites. The 

control device inlet sampling site for 

determination of vent stream molar 

composition or TOC (less methane 

and ethane) reduction efficiency shall 

be prior to the inlet of the control 

device and after the recovery system. 

(2) Method 2. 2A, 2C, or 2D, as appropriate, for determination of the gas 

volumetric flow rates. 

(3) The emission rate correction 

factor, integrated sampling and analysis procedure of Method 3 shall be 

used to determine the oxygen concentration (%Ou) for the purposes of determining compliance with the 20 

ppmv limit. The sampling site shall be 

the same as that of the TOC samples, 

and the samples shall be taken during 

the same time that the TOC samples 

are taken. 

The TOC concentration corrected to 

3 percent 0> (Ce) shall be computed 

using the following equation: 

Ce — Croc 

17.9 

20.9-%O M 

where: 

C,=Concentration of TOC corrected to 3 

percent Ot, dry basis, ppm by volume. 

Croc=Concentration of TOC (minus methane and ethane), dry basis, ppm by 

volume. 

%On=Coneentratlon of O,. dry basis, percent by volume. 

(4) Method 18 to determine the concentration of TOC in the control 

device outlet and the concentration of 

TOC in the inlet when the reduction 

40 CFR Ch. I (7-1-91 Edition) 

efficiency of the control device is to be 

determined. 

(i) The sampling time for each run 

shall be 1 hour in which either an integrated sample or four grab samples 

shall be taken. If grab sampling is 

used then the samples shall be taken 

at 15-minute intervals. 

(il) The emission reduction (R) of 

TOC (minus methane and ethane) 

shall be determined using the following equation: 

E.-E. 

E, 

X100 

where: 

R=Emission reduction, percent by weight. 

E,=Mass rate of TOC entering the control 

device, kg TOC/hr. 

E„=Mass rate of TOC discharged to the atmosphere, kg TOC/hr. 

(iii) The mass rates of TOC (E,, E„) 

shall be computed using the following 

equations: 

••A CuAtlu 

1=1 ¥ 

a 

E„=KJ I C«MJQ. 

where: 

C„. C„=Concentration of sample component 

"j" of the gas stream at the inlet and 

outlet of the control device, respectively, 

dry basis, ppm by volume. 

Mu, M*=Molecular weight of sample component "J" of the gas stream at the Inlet 

and ouUet of the control device, respectively, g/g-mole (lb/lb-mole). 

Qi. Q.=Flow rate of gas stream at the Inlet 

and outlet of the control device, respectively, dscm/mln (dscf/hr). 

K,=Constant, 2.494x10"* (1/ppm) (g-mole/ 

scm) (kg/g) (mln/hr), where standard 

temperature for (g-mole/scm) Is 20 *C. 

(iv) The TOC concentration (Croc) is 

the sum of the individual components 

and shall be computed for each run 

using the following equation: 

620 

Environmental Protection Agency 

CTOCS 

n 

X C, 

J = l 

where: 

Croc=Concentration of

 TOC (minus methane and ethane), dry basis, ppm by 

volume. 

C,=Concentration of sample components 

"J", dry basis, ppm by volume. 

n=Number of components ln the sample. 

(5) When a boiler or process heater 

with a design heat input capacity of 44 

MW (150 million Btu/hour) or greater 

is used to seek to comply with 

{ 60.662(a), the requirement for an initial performance test is waived, in accordance with { 60.8(b). However, the 

Administrator reserves the option to. 

require testing at such other times as 

may be required, as provided for in 

section 114 of the Act. 

(c) When a flare is used to seek to 

comply with S 60.662(b), the flare shall 

comply with the requirements of 

S 60.18. 

(d) The foUowing test methods in 

appendix A to this part, except as provided under { 60.8(b), shall be used for 

determining the net heating value of 

the gas combusted to determine compliance under {60.662(b) and for determining the process vent stream 

TRE index value to determine compliance under { 60.662(c). 

(D(i) Method 1 or IA, as appropriate, for selection of the sampling site. 

The sampling site for the vent stream 

flow rate and molar composition determination prescribed in { 60.664(d) (2) 

and (3) shall be, except for the situations outlined in paragraph (d)(1)(H) 

of this section, prior to the inlet of 

any control device, prior to any postdistillation dilution of the stream with 

air, and prior to any post-distillation 

introduction of halogenated compounds into the process vent stream. 

No transverse site selection method Is 

needed for vents smaller than 4 inches 

in diameter. 

(il) If any gas stream other than the 

distillation vent stream from the affected facility is normally conducted 

through the final recovery device. 

(A) The sampling site for vent 

stream flow rate and molar composi-

§60.664 

tion shall be prior to the final recovery device and prior to the point at 

which the nondistillation stream Is introduced. 

(B) The efficiency of the final recovery device is determined by measuring 

the TOC concentration using Method 

18 at the inlet to the final recovery 

device after the introduction of any 

nondistillation vent stream and at the 

outlet of the final recovery device. 

(C) This efficiency is applied to the 

TOC concentration measured prior to 

the final recovery device and prior to 

the Introduction of the nondistillation 

stream to determine the concentration 

of TOC in the distillation vent stream 

from the final recovery device. This 

concentration of TOC is then used to 

perform the calculations outlined in 

{ 60.664(d) (4) and (5). 

(2) The molar composition of the 

process vent stream shall be determined as f oUows: 

(1) Method 18 to measure the concentration of TOC including those 

containing halogens. 

(ii) ASTM D1946-77 (incorporation 

by reference as specified in { 60.17 of 

this part) to measure the concentration of carbon monoxide and hydrogen. 

(iii) Method 4 to measure the content of water vapor. 

(3) The volumetric flow rate shall be 

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

2D, as appropriate. 

(4) The net heating value of the vent 

stream shall be calculated using the 

foUowing equation: 

n 

HT=K, j X QH, j 

where: 

HT=Net heating value of the sample. MJ/ 

scm. where the net enthalpy per mole of 

vent stream Is based on combustion at 

25 *C and 760 mm Hg, but the standard 

temperature for determining the volume 

corresponding to one mole Is 20*C, as in 

the definition of Q. (vent stream flow 

rate). 

K.=Constant, 1.740 x 10"' 

621 

,1 --Ji 

v •if 

V 
*aa»3»:gft.jy Jp-jl 

§60.664 

(1) (g-mole) (MJ). 

ppm scm kcal 

where standard temperature for 

(g-mole) 

Is 20 *C. 

C,=Concentration on a wet basis of compound ] ln ppm, as measured for organics by Method 18 and measured for hydrogen and carbon monoxide by ASTM 

D1946-77 (Incorporation by reference as 

specified ln . 60.17 of this part) as Indicated ln S 60.664(d)(2). 

H,=Net heat of combustion of compound J, 

kcal/g-mole, based on combustion at 25 

*C and 760 mm Hg. 

The heats of combustion of vent 

stream components would be required 

to be determined using ASTM D2382-

76 (incorporation by reference as specified in {60.17 of this part) if published values are not available or 

cannot be calculated. 

(5) The emission rate of TOC in the 

vent stream shall be calculated using 

the following equation: 

Eroc=Ki X CM, 

J = l 

Q. 

where: 

40 CFR Ch. I (7-1-91 Edition) 

Era=Emission rate of TOC ln the sample, 

kg/hr. 

K.=Constant, 2.494x10'' (1/ppm) (g-mole/ 

scm) (kg/g) (mln/hr). where standard 

temperature for (g-mole/scm) is 20 'C. 

C,=Concentration on a basis of compound J 

ln ppm as measured by Method 18 as Indicated ln 3 60.664(d)(2). 

M,=Molecular weight of sample J, g/g-mole. 

Q.=Vent stream flow rate (scm/mln) at a 

temperature of 20 *C. 

(6) The total process vent stream 

concentration (by volume) of compounds containing halogens (ppmv, by 

compound) shall be summed from the 

Individual concentrations of compounds containing halogens which 

were measured by Method 18. 

(e) For purposes of complying with 

{ 60.662(c) the owner or operator of a 

facility affected by this subpart shall 

calculate the TRE index value of the 

vent stream using the equation for incineration ln paragraph (e)(1) of this 

section for halogenated vent streams. 

The owner or operator of an affected 

facility with a nonhalogenated vent 

stream shall determine the TRE index 

value by calculating values using both 

the incinerator equation in (e)(1) and 

the flare equation ln (e)(2) of this section and selecting the lower of the two 

values. 

(1) The equation for calculating the 

TRE index value of a vent stream controlled by an incinerator is as follows: 

622 

Environmental Protection Agency §60.664 

+ 

a 

m 

iff r 

a 

3 

+ 

•o 

+ 

3 

•B 

+ 

+ 

rv. 

• 3 1 

fm. 

-N 

af 

623 
§60.664 

(i) where for a vent stream flow rate 

(scm/min) at a standard temperature 

of 20 *C that is greater than or equal 

to 14.2 scm/min: 

TRE=TRE Index value. 

Q.=Vent stream flow rate (scm/min) at a 

standard temperature of 20 "C. 

HT=Vent stream net heating value (MJ/ 

scm), where the net enthalpy per mole 

of vent stream is based on combustion at 

25 'C and 760 mm Hg, but the standard 

temperature for determining the volume 

corresponding to one mole Is 20 *C as ln 

the definition of Q.. 

40 CFR Ch. I (7.1-91 Edition) 

Y,=Q. for all vent stream categories listed 

ln Table 1 except for Category E vent 

;

 streams where Y,=(Q.) (HT)/3.6. 

ETOC=Hourly emissions of TOC reported in 

kg/hr. 

a, b, c, d, e, and f are coefficients. 

T he set of coefficients that apply to 

a vent stream can be obtained from 

Table 1. 

Environmental Protection Agency § 60.664 

TABLE 1. DISTILLATION USPS TRE COEFFICIENTS FOR VENT STREAMS CONTROLLED BY AN INCINERATOR 

DESIGN CATEGORY Al . FOR HALOGENATED PROCESS VE 

Qs •> Vent Stream Flow rate 

(son/mln) 

14.2 « 0 . < 18.8 

18.8 < 0 i < 699 

699 < 0 ! < 1400 

1400 < Q, < 2100 

2100 < Oi < 2800 

2800 < Q, < 3500 

a 

19.18370 

20.00S63 

39.67022 

59.73481 

79.59941 

99.46400 

NT STREAMS. 

b 

0.27580 

0.27580 

0.29973 

0.31467 

0.32572 

0.33456 

IF 0 < NET KEATING VALUE (MJ/scm) < 

c 

0.75762 

0.30387 

0.30387 

0.30387 

0.30387 

0.30387 

d 

-0.13064 

-0.13064 

-0.13064 

-0.13064 

-0.13064 

-0.13064 

e 

0 

0 

0 

0 

0 

0 

3.5. 

• 1 

0.01025 

0.01025 

0.01449 

0.01775 

0.02049 

0.02291 

0ESI6N CATEGORY A2. FOR HALOGENATED PROCESS VENT STREAMS. 

Q, - Vent St rem Flow rate 

(son/ml nl 

14.2 « 9, < 18.8 

18.8 < OJ < 699 

699 < Q: < 1400 

1400 < Q. < 2100 

2800 < 9, < 3500 

a 

18.84466 

19.66658 

39.19213 

58.71768 

78.24323 

97.76879 

b 

0.26742 

0.26742 

0.29062 

0.30511 

0.31582 

0.32439 

IF NET HEATING VALUE > 

c 

-0.20044 

-0.25332 

-0.25332 

-0.25332 

-0.25332 

-0.25332 

d 

1 oooooo 

3.5 MJ/scm: 

e oooooo 1 f 

0.01025 

0.01025 

0.01449 

0.0177S 

0.02049 

0.02291 

DESIGN CATEGORY B. FOR N0NHAL0GENATE0 PROCESS VENT STREAMS. IF 0 < NET HEAT1N6 VALUE (MJ/scm) « 0.48: 

Q. • Vent Stream Flow rate 

(scm/min) 

14.2 < Qs < 1340 

1340 < Q. « 2690 

2630 < Q, < 4040 

a 

8.54245 

16.94386 

25.34528 

b 

0.10555 

0.11470 

0.12042 

c 

0.09030 

0.09030 

0.09030 

d 

-0.17109 

-0.17109 

-0.17109 

e 

j OOO 

f 

0.0102S 

0.01449 

0.01775 

624 

DESIGN CATEGORY C. FOR NONHALOGENATED PROCESS VENT STREAMS 

Qs - Vent Stream Flow rate 

( scm/min] 

14.2 < q , < 1340 

1340 < Ql < 2690 

2690 < Q, < 4040 

a 

9.25233 

18.36363 

27.47492 

b 

0.06105 

0.06635 

0.06965 

. IF 0.48 < 

c 

0.31937 

0.31937 

0.31937 

NET HEATING VALUE (MJ/scm) < 1.9: 

d 

-0.16181 

-0.16161 

-0.16161 

e 

0 

0 

0 

f 

0.01025 

0.01449 

0.01775 

DESIGN CATEGORY 0. FOR NONHALOGENATED PRKESS VENT STREAMS. IF 1.9 < NET HEATING VALUE (MJ/scm) < 3.6: 

Q. • Vent Stream Flow rate 

(scm/min) 

14.2 < 9. < 1180 

1180 < Q, < 2370 

2370 < 9 | < 3550 

a 

6.67868 

13.21633 

19.75398 

b 

0.06943 

0.07546 

0.07922 

c 

0.02562 

0.02582 

0.02582 

d 

0 

0 

0 

e 

0 

0 

0 

f 

0.01025 

0.01449 

0.01775 

DESIGN CATEGORY E. FOR NONHALOGENATED PROCESS VENT STREAMS. IF NET HEATING VALUE > 3.6 MJ/scm: 

Y, - Dilution Flow rate 

(sctl/mln) - (0. ) (Hrl/3. 6 

14.2 < Y, < 1180 

1180 < Y! < 2370 

2370 < l\ < 3550 

a 

6.67868 

13.21633 

19.75398 

b 

0 

0 

0 

c OOO d 

-0.00707 

-0.00707 

-0.00707 

e 

0.02220 

0.02412 

0.02533 

f 

0.01025 

0.01449 

0.01775 

625 
§60.664 

(ii) where for a vent stream flow rate 

(scm/min) at a standard temperature 

of 20 *C that is less than 14.2 scm/min: 

TRE=TRE Index value. 

Q,=14.2 scm/min. 

HT=(PLOWKHVAL)/14.2. 

where by the following inputs are 

used: 

FLOW=Vent stream flow rate (scm/min), 

at a standard temperature of 20 *C. 

HVAL=Vent stream net heating value (MJ7 

scm), where the net enthalpy per mole 

of vent stream is based on combustion at 

25 'C and 760 mm Hg, but the standard 

temperature for determining the volume 

corresponding to one mole Is 20 'C as in 

definition of Q.. 

40 CFR Ch. I (7-1-91 Edition) 

Y.= 14.2 scm/min for all vent stream categories listed in Table 1 except for Category 

• E vent streams, where Y.=(14.2XHT)/ 

3.6. 

Eras Hourly emissions of TOC reported ln 

kg/hr. 

a, b, c, d, e, and f are coefficients. 

The set of coefficients that apply to 

a vent stream can be obtained from 

Table 1. 

(2) The equation for calculating the 

TRE index value of a vent stream controlled by a flare is as follows: 

TRE = • 

Eroc 

[a(ci)+b(Q.)"+c(Q.)(HT)+d(EIOC)-re] 

a, b, c, d. and e are coefficients. 

The set of coefficients that apply to 

a vent stream shall be obtained from 

Table 2. 

where: 

TRE=TRE Index value. 

Eroc=Hourly emission rate of TOC reported 

in kg/hr. 

Q.=Vent stream flow rate (scm/min) at a 

standard temperature of 20 *C. 

Ht=Vent stream net heating value (MJ7 

scm) where the net enthalpy per mole of 

offgas is based on combustion at 25 *C 

and 760 mm Hg, but the standard temperature for determining the volume 

corresponding to one mole is 20 "C as in 

the definition of Q.. 

TABLE 2—DISTILLATION NSPS TRE COEFFICIENTS FOR VENT STREAMS CONTROLLED BY A FLARE 

H, <11.2 MJ/scm 

H, >11.2 MJ/scm 

a 

2.25 

0.309 

b 

0.288 

0.0619 

c 

-0.193 

-0.0043 

d 

-0.0051 

-0.0034 

e 

2.08 

2.08 

(f) Each owner or operator of an affected facility seeking to comply with 

S 60.660(c)(4) or § 60.662(c) shall recalculate the TRE Index value for that 

affected facility whenever process 

changes are made. Examples of process changes include changes in production capacity, feedstock type, or catalyst type, or whenever there is replacement, removal, or addition of recovery 

equipment. The TRE index value shall 

be recalculated based on test data, or 

on best engineering estimates of the 

effects of the change to the recovery 

system. 

(1) Where the recalculated TRE 

index value is less than or equal to 1.0, 

the owner or operator shall notify the 

Administrator within 1 week of the recalculation and shall conduct a performance test according to the methods and procedures required by 

! 60.664 ln order to determine compliance with $60.662(a). Performance 

tests must be conducted as soon as 

possible after the process change but 

626 

Environmental Protection Agency 

no later than 180 days from the time 

of the process change. 

(2) Where the initial TRE index 

value is greater than 8.0 and the recalculated TRE index value Is less than 

or equal to 8.0 but greater than 1.0, 

the owner or operator shall conduct a 

performance test in accordance with 

55 60.8 and 60.664 and shall comply 

with SS 60.663, 60.664 and 60.665. Performance tests must be conducted as 

soon as possible after the process 

change but no later than 180 days 

from the time of the process change. 

(g) Any owner or operator subject to 

the provisions of this subpart seeking 

to demonstrate compliance with 

S 60.660(c)(6) shall use Method 2, 2A, 

2C, or 2D as appropriate, for determination of volumetric flow rate. 

§60.665 Reporting and recordkeeping requirements. 

(a) Each owner or operator subject 

to S 60.662 shall notify the Administrator of the specific provisions of 

S 60.662 (S 60.662 (a), (b), or («) with 

which the owner or operator has elected to comply. Notification shall be 

submitted with the notification of initial start-up required by $ 60.7(a)(3). If 

an owner or operator elects at a later 

date to use an alternative provision of 

$60,662 with which he or she will 

comply, then the Administrator shall 

be notified by the owner or operator 

90 days before implementing a change 

and, upon implementing the change, a 

performance test shall be performed 

as specified by $60,664 within 180 

days. 

(b) Each owner or operator subject 

to the provisions of this subpart shall 

keep an up-to-date, readily accessible 

record of the following data measured 

during each performance test, and also 

Include the following data in the 

report of the initial performance test 

required under $ 60.8. Where a boiler 

or process heater with a design heat 

input capacity of 44 MW (150 million 

Btu/hour) or greater is used to comply 

with $ 60.662(a), a report containing 

performance test data need not be submitted, but a report containing the information in 5 60.665(b)(2)(l) is required. The same data specified in this 

section shall be submitted in the reports of all subsequently required per-

§60.665 

formance tests where either the emission control efficiency of a control 

device, outlet concentration of TOC, 

or the TRE index value of a vent 

stream from a recovery system Is determined. 

(1) Where an owner or operator subject to the provisions of this subpart 

seeks to demonstrate compliance with 

$ 60.662(a) through use of either a 

thermal or catalytic incinerator: 

(i) The average firebox temperature 

of the incinerator (or the average temperature upstream and downstream of 

the catalyst bed for a catalytic incinerator), measured at least every 15 minutes and averaged over the same time 

period of the performance testing, and 

(ii) The percent reduction of TOC 

determined as specified in $ 60.664(b) 

achieved by the incinerator, or the 

concentration of TOC (ppmv, by compound) determined as specified in 

$ 60.664(b) at the outlet of the control 

device on a dry basis corrected to 3 

percent oxygen. 

(2) Where an owner or operator subject to the provisions of this subpart 

seeks to demonstrate compliance with 

$ 60.662(a) through use of a boiler or 

process heater: 

(i) A description of the location at 

which the vent stream is introduced 

into the boiler or process heater, and 

(ii) The average combustion temperature of the boiler or process heater 

with a design heat input capacity of 

less than 44 MW (150 million Btu/hr) 

measured at least every 15 minutes 

and averaged over the same time 

period of the performance testing. 

(3) Where an owner or operator subject to the provisions of this subpart 

seeks to demonstrate compliance with 

3 60.662(b) through use of a smokeless 

flare, flare design (i.e., steam-assisted, 

air-assisted or nonasslsted). all visible 

emission readings, heat content determinations, flow rate measurements, 

and exit velocity determinations made 

during the performance test, continuous records of the flare pilot flame 

monitoring, and records of all periods 

of operations during which the pilot 

flame is absent. 

(4) Where an owner or operator subject to the provisions of this subpart 

seeks to demonstrate compliance with 

$ 60.662(c): 

627 

* -X9 

£'tS 

3-
§60.665 

(i) Where an absorber is the final recovery device in the recovery system, 

the exit specific gravity (or alternative 

parameter which is a measure of the 

degree of absorbing liquid saturation, 

lf approved by the Administrator), and 

average exit temperature, of the adsorbing liquid measured at least every 

15 minutes and averaged over the 

same time period of the performance 

testing (both measured while the vent 

stream is normally routed and constituted), or 

(ii) Where a condenser is the final 

recovery device in the recovery 

system, the average exit (product side) 

temperature measured at least every 

15 minutes and averaged over the 

same time period of the performance 

testing while the vent stream is routed 

and constituted normally, or 

(iii) Where a carbon adsorber is the 

final recovery device in the recovery 

system, the total steam mass flow 

measured at least every 15 minutes 

and averaged over the same time 

period of the performance test (full 

carbon bed cycle), temperature of the 

carbon bed after regeneration (and 

within 15 minutes of completion of 

any cooling cycle(s)). and duration of 

the carbon bed steaming cycle (all 

measured while the vent stream is 

routed and constituted normally), or 

(iv) As an alternative to 

S 60.665(b)(4) (d), (il) or (Iii), the concentration level or reading indicated 

by the organics monitoring device at 

the outlet of the absorber, condenser, 

or carbon adsorber, measured at least 

every 15 minutes and averaged over 

the same time period of the performance testing while the vent stream is 

normally routed and constituted. 

(v) All measurements and calculations performed to determine the TRE 

Index value of the vent stream. 

(c) Each owner or operator subject 

to the provisions of this subpart shall 

keep up-to-date, readily accessible continuous records of the equipment operating parameters specified to be 

monitored under $ 60.663 (a) and (c) as 

well as up-to-date, readily accessible 

records of periods of operation during 

which the parameter boundaries established during the most recent performance test are exceeded. The Administrator may at any time require a 

40 CFR Ch. I (7-1-91 Edition) 

report of these data. Where a combustion device is used to comply with 

$ 60.662(a), periods of operation 

during which the parameter boundaries established during the most 

recent performance tests are exceeded 

are defined as follows: 

(1) For thermal incinerators, all 3-

hour periods of operation during 

which the average combustion temperature was more than 28 *C (50 *F) 

below the average combustion temperature during the most recent performance test at which compliance with 

$ 60.662(a) was determined. 

(2) For catalytic incinerators, all 3-

hour periods of operation during 

which the average temperature of the 

vent stream immediately before the 

catalyst bed is more than 28 *C (50 *F) 

below the average temperature of the 

vent stream during the most recent 

performance test at which compliance 

with $ 60.662(a) was determined. The 

owner or operator also shall record all 

3-hour periods of operation during 

which the average temperature difference across the catalyst bed is less 

than 80 percent of the average temperature difference of the device 

during the most recent performance 

test at which compliance with 

$ 60.662(a) was determined. 

(3) All 3-hour periods of operation 

during which the average combustion 

temperature was more than 28 *C (50 

*F) below the average combustion temperature during the most recent performance test at which compliance 

with $ 60.662(a) was determined for 

boilers or process heaters with a 

design heat input capacity of less than 

44 MW (150 million Btu/hr). 

(4) For boilers or process heaters, 

whenever there is a change in the location at which the vent stream is introduced into the flame zone as required under $ 60.662(a). 

(d) Each owner or operator subject 

to the provisions of this subpart shall 

keep up to date, readily accessible continuous records of the flow indication 

specified under $ 60.663(a)(2). 

$ 60.663(b)(2) and $ 60.663(c)(1), as 

well as up-to-date, readily accessible 

records of all periods when the vent 

stream is diverted from the control 

device or has no flow rate. 

628 

Environmontal Protection Agency 

(e) Each owner or operator subject 

to the provisions of this subpart who 

uses a boiler or process heater with a 

design heat input capacity of 44 MW 

or greater to comply with $ 60.662(a) 

shall keep an up-to-date, readily accessible record of all periods of operation 

of the boiler or process heater. (Examples of such records could include 

records of steam use, fuel use, or monitoring data collected pursuant to other 

State or Federal regulatory requirements.) 

(f) Each owner or operator subject 

to the provisions of this subpart shall 

keep up-to-date, readily accessible continuous records of the flare pilot flame 

monitoring specified under $ 60.663(b), 

as well as up-to-date, readily accessible 

records of all periods of operations in 

which the pilot flame is absent. 

(g) Each owner or operator subject 

to the.provisions of this subpart shall 

keep up-to-date, readily accessible continuous records of the equipment operating parameters specified to be 

monitored under $ 60.663(d), as well as 

up-to-date, readily accessible records 

of periods of operation during which 

the parameter boundaries established 

during the most recent performance 

test are exceeded. The Administrator 

may at any time require a report of 

these data. Where an owner or operator seeks to comply with $ 60.662(c), 

periods of operation during which the 

parameter boundaries established 

during the most recent performance 

tests are exceeded are defined as follows: 

(1) Where an absorber is the final recovery device in a recovery system, 

and where an organic compound monitoring device is not used: 

(i) All 3-hour periods of operation 

during which the average absorbing 

liquid temperature was more than 11 

*C (20 *F) above the average absorbing 

liquid temperature during the most 

recent performance test, or 

(ii) All 3-hour periods of operation 

during which the average absorbing 

liquid specific gravity was more than 

0.1 unit above, or more than 0.1 unit 

below, the average absorbing liquid 

specific gravity during the most recent 

performance test (unless monitoring 

of an alternative parameter, which is a 

measure of the degree of absorbing 

§60.665 

liquid saturation, is approved by the 

Administrator, in which case he will 

define appropriate parameter boundaries and periods of operation during 

which they are exceeded). 

(2) Where a condenser is the final 

recovery device in a system, and where 

an organic compound monitoring 

device is not used, all 3-hour periods of 

operation during which the average 

exit (product side) condenser operating temperature was more than 6 *C (1 

l'F) above the average exit (product 

side) operating temperature during 

the most recent performance test. 

(3) Where a carbon adsorber is the 

final recovery device in a system, and 

where an organic compound monitoring device Is not used: 

(I) All carbon bed regeneration 

cycles during which the total mass 

steam flow was more than 10 percent 

below the total mass steam flow 

during the most recent performance 

test, or 

(II) All carbon bed regeneration 

cycles during which the temperature 

of the carbon bed after regeneration 

(and after completion of any cooling 

cycle(s)) was more than 10 percent 

greater than the carbon bed temperature (in degrees Celsius) during the 

most recent performance test. 

(4) Where an absorber, condenser, or 

carbon adsorber is the final recovery 

device in the recovery system and 

where an organic compound monitoring device is used, all 3-hour periods of 

operation during which the average 

organic compound concentration level 

or reading of organic compounds in 

the exhaust gases is more than 20 percent greater than the exhaust gas organic compound concentration level or 

reading measured by the monitoring 

device during the most recent performance test. 

(h) Each owner or operator of an affected facility subject to the provisions 

of this subpart and seeking to demonstrate compliance with $ 60.662(c) 

shall keep up-to-date, readily accessible records of: 

(1) Any changes ln production capacity, feedstock type, or catalyst type, or 

of any replacement, removal or addition of recovery equipment or a distillation unit; 

H| i 

HI 

..4 ' 

V 1 

629 
§60.665 

(2) Any recalculation of the TRE 

index value performed pursuant to 

S 60.664(f); and 

(3) The results of any performance 

test performed pursuant to the methods and procedures required by 

5 60.664(d). 

(1) Each owner or operator of an affected facility that seeks to comply 

with the requirements of this subpart 

by complying with the flow rate cutoff 

in $ 60.660(c)(6) shall keep up-to-date, 

readily accessible records to indicate 

that the vent stream flow rate is less 

than 0.008 m'/min and of any change 

ln equipment or process operation 

that increases the operating vent 

stream flow rate, including a measurement of the new vent stream flow rate. 

(j) Each owner or operator of an affected facility that seeks to comply 

with the requirements of this subpart 

by complying with the design production capacity provision in 

S 60.660(c)(5) shall keep up-to-date, 

readily accessible records of any 

change in equipment or process operation that increases the design production capacity of the process unit in 

which the affected facility Is located. 

(k) Each owner and operator subject 

to the provisions of this subpart is 

exempt from the quarterly reporting 

requirements contained ln $ 60.7(c) of 

the General Provisions. 

(1) Each owner or operator that 

seeks to comply with the requirements 

of this subpart by complying with the 

requirements of $ 60.660 (c)(4), (c)(5), 

or (c)(6) or $ 60.662 shall submit to the 

Administrator semiannual reports of 

the foUowing recorded Information. 

The initial report shall be submitted 

within 6 months after the initial startup date. 

(1) Exceedances of monitored parameters recorded under $ 60.665 (c) 

and (g). 

(2) All periods recorded under 

$ 60.665(d) when the vent stream is diverted from the control device or has 

no flow rate. 

(3) All periods recorded under 

$ 80.665(e) when the boiler or process 

heater was not operating. 

(4) All periods recorded under 

$ 60.665(f) in which the pilot flame of 

the flare was absent. 

40 CFR Ch. I (7-1-91 Edition) 

(5) Any change in equipment or 

process operation that Increases the 

operating vent stream flow rate above 

the low flow exemption level In 

$60,660(0(6), including a measurement of the new vent stream flow rate, 

as recorded under $ 60.665(1). These 

must be reported as soon as possible 

after the change and no later than 180 

days after the change. A performance 

test must be completed with the same 

time period to verify the recalculated 

flow value and to obtain the vent 

stream characteristics of heating value 

and Eroc. The performance test Is subject to the requirements of $ 60.8 of 

the General Provisions. Unless the facility qualifies for an exemption under 

the low capacity exemption status in 

$ 60.660(c)(5), the facility must begin 

compliance with the requirements set 

forth in $ 60.662. 

(6) Any change in equipment or 

process operation, as recorded under 

$60.665(j), that increases the design 

production capacity above the low capacity exemption level in $ 60.660(c)(5) 

and the new capacity resulting from 

the change for the distillation process 

unit containing the affected facility. 

These must be reported as soon as possible after the change and no later 

than 180' days after the change. A performance test must be completed 

within the same time period to obtain 

the vent stream flow rate, heating 

value, Ene. The performance test is 

subject to the requirements of $ 60.8 

of the General Provisions. Unless the 

facility qualifies for an exemption 

under the low flow exemption ln 

$60,660(0(6). the faculty must begin 

compliance with the requirements set 

forth in $ 60.662. 

(7) Any recalculation of the TRE 

Index value, as recorded under 

$ 60.665(h). 

(m) The requirements of $60,665(1) 

remain ln force until and unless EPA, 

in delegating enforcement authority 

to a State under section 111(c) of the 

Act, approves reporting requirements 

or an alternative means of compliance 

surveillance adopted by such State. In 

that event, affected sources within the 

State will be relieved of the obligation 

to comply with $ 60.665(1), provided 

that they comply with the requirements established by the State. 

630 

Environmental Protection Agency 

(n) Each owner or operator that 

seeks to demonstrate compliance with 

$ 60.660(c)(5) must submit to the Administrator an Initial report detailing 

the design production capclty of the 

process unit. 

(o) Each owner or operator that 

seeks to demonstrate compliance with 

$ 60.660(c)(6) must submit to the Administrator an initial report Including 

a flow rate measurement using the 

test methods specified ln $ 60.664. 

(p) The Administrator will specify 

appropriate reporting and recordkeeping requirements where the owner or 

operator of an affected facility compiles with the standards specified 

under $ 60.662 other than as provided 

under $ 60.663(a), (b). (c) and (d). 

[55 FR 26922. June 29, 

Sept. 7.1990] 1990; 55 FR 36932, 

S 60.666 Reconstruction. 

For purposes of this subpart "fixed 

capital cost of the new components," 

as used ln $ 60.15, Includes the fixed 

capital cost of all depreciable components which are or will be replaced 

pursuant to all continuous programs 

of component replacement which are 

commenced within any 2-year period 

following December 30, 1983. For purposes of this paragraph, "commenced" 

means that an owner or operator has 

undertaken a continuous program of 

component replacement or that an 

owner or operator has entered into a 

contractual obligation to undertake 

and complete, within a reasonable 

time, a continuous program of component replacement. 

(Approved by the Office of Management 

and Budget under control number 2060-

0055) 

§60.667 Chemicals affected by subpart 

NNN. 

Chemical name 

Acetaldehyde 

Acetaldol 

Acetic add 

Acetic anhydride 

Acetone 

Acetone cyanohydrtn. 

Acetylene 

Acrylic add 

Acrytomtrile 

Adkxcedd 

60-140 O—91-

CASNo.* 

75-07-0 

107-89-1 

64-19-7 

108-24-7 

67-84-1 

75-88-5 

74-88-2 

79-10-7 

107-13-1 

124-04-9 

§60.667 

Chemical name 

AcSponftrlle 

Alcohols, C-11 or lower, mixtures.... 

Alcohols, C-12 or higher, mixtures.. 

APyl chloride 

Amylene 

AnOne... 

Benzenesulfonic add 

Benzenesuttonlc add C,n«-alkyl derivatives, 

•odium salts 

Benzoic add, tech.. 

Benzyl chloride... 

Blphenyl.. 

Brsphend A 

Bromotone 

1 ,3-ButatSene 

Butaolene and butane fractions... 

rvButane... 

1,4-ButanecSol.... 

Butanes, mbced.. 

1 .Butane 

2-Butene. 

Butanes, mbced.. 

ivButyl acetate... 

Butyl acrylate... 

rvButyl alcohol 

sec-Butyl alcohol... 

tart-Butyl alcohol.. 

Butytbenzyl phthalate.. 

Butylena glycol.. 

tart-Butyl hydroperoxide... 

2-Butym-l .4-oSol 

Butyraldahyoa... 

Butyric anhydride.. 

Caprolactam.. 

Carbon drsutfido 

Carbon tetrabromlde 

Carbon tetrachloride 

Chlorobenzena 

2<Moro-MethytanikK>)4^1aapropy1ainlnor«. 

triazlne 

Chloroform. 

pChloronltrobenzeiie 

CBric add 

Crotonalderryde 

Crotonlc add 

Cumene— 

Cumene hydroporojudo •• 

Cyenuric chloride.— 

Cydohexane.. 

Cydohexane, oxkftzed.., 

Cyclohexanol 

Cydohexanone... 

Cydohexanone oxtme.. 

Cydohexane 

1.3-CyclopGntadtane 

Cyclopropane 

Diacetone alcohol.. 

Drbutantzed aromatic concentrate.., 

1,4-Oichlorobutene... 

3.4-OtcMoro-l-butene 

Uchtorodlfiuoromeihane.. 

OiehtoodlrTiettrylallano 

Dtehloiorluoruriieihane 

-Oichlorohydrln 

Diethanolamine 

Dterhylbenzene... 

Diethylene glycol 

Dl-rvheptyl-n-nonyl undecyl phthalate... 

OMeodacyt phthalate 

OSaononyl phthalate 

CAS No.* 

107-05-1 

513-35-9 

62-53-3 

71-43-2 

98-11-3 

88081-81-2 

85-85-0 

100-44-7 

92-62-4 

80-05-7 

76-08-4 

108-99-0 

108-87-6 

110-63-4 

108-96-8 

25167-87-3 

123-86-4 

141-32-2 

71-38-3 

78-92-2 

75-65-0 

85-68-7 

107-68-0 

75-61-2 

110-65-8 

123-72-8 

106-31-0 

105-60-2 

75-15-0 

558-13-4 

56-23-5 

106-00-7 

1912-24-6 

87-68-3 

100-00-5 

77-82-8 

4170-30-0 

3724-65-0 

80-15-9 

108-77-0 

110-82-7 

68512-15-2 

108-93-0 

108-94-1 

100-64-1 

110-63-8 

542-92-7 

75-19-4 

123-42-2 

110-67-8 

64037-54-3 

75-71-8 

75-76-5 

75-43-4 

96-23-1 

111-42-2 

25340-17-4 

111-48-6 

65-68-7 

26761-40-0 

28553-12-0 

631 
§60.668 

Chemical name 

DfnwttiyteVnns 

Dimethyl terephthalate.. 

2,4-Omrtrotocuene.. 

2.4-(end 2.6rOTnltTOto(uor»... 

Dioctyl phthalata 

Dodecene 

Dodecylbanzene, non linear 

Dodecylbenzenesutfonjc add 

Dodecylbenzenesunonic add, sodium salt... 

EpicNcrohydrfn 

Ethanol 

Ethanoiamtne 

Ethyl acetate 

Ethyl ecrylate 

Ethylbenzene 

Ethyl chloride 

Ethyl cyanide 

Ethylene 

Ethylene ctoromkte 

Ethylene dichloride 

Ethylene glycol.. 

Ethylene Qtyod monobutyl... 

Ethylene gtyod monoethyt ether 

Ethylene gtyod monoethyl ether acetate.. 

Ethylene glyod monomethyl ether 

Ethylene oxide 

2-Ethythexanal 

2-Ethyrhexyl alcohol 

(2-Ethythexyl) amine 

Et* 

6-EmyM,2,3.4-tetrahydro 9,10-*ntrsceneo»one. 

Formaldehyde. 

Glycerol 

(mbced)... 

. . . . * • • * 

rrexeoocyi craonoe 

Hexamethylene diamine 

Hexamethylene dramlne arJpate... 

Haxamethylenetttti amine 

Hexane 

2-r 

Hydrogen cyanide... 

Isobutane 

Isobutand 

rsobutyteno 

laobytyi aldehyde 

laodecyl alcohol 

Isooctyl alcohd 

laopenlane 

laophthafic add 

laoprene 

Ketone 

Linear alcohols, ethoxytated. mixed 

Linear aloohofa, ethoxylated. and 

sodrum salt, mixed... 

Linear alcohols, sulfated, sodium salt, mixed.. 

Linear affcybenzene , 

Magnesium acetate . 

Maleic anhydride 

Meiamine 

Methacrylonltrile.. 

Methanol 

Methylamine 

ar-Merhytoenzonedlamine... 

Methyl chloride 

Methylene chloride 

Methyl ethyl ketone 

Methyl iodrde.. 

Methyl Isobutyl ketone.. 

124-40-3 

120-61-6 

121-14-2 

121-14-2 

608-20-2 

117-81-7 

25378-22-7 

27176-87-0 

25155-30-0 

106-89-8 

64-17-5 

141-43-5 

141-78-6 

140-88-5 

100-41-4 

75-00-3 

107-12-0 

74-85-1 

106-93-4 

107-06-2 

107-21-1 

111-76-2 

110-80-5 

111-15-9 

109-88-4 

75-21-8 

26268-68-2 

104-76-7 

104-75-6 

25550-14-5 

15547-17-8 

50-00-0 

56-61-5 

142-82-5 

124-09-4 

3323-53-3 

100-97-0 

110-54-3 

13042-02-9 

1119-85-3 

74-90-8 

75-28-5 

78-83-1 

115-11-7 

76-84-2 

25338-17-7 

28952-21-6 

78-78-4 

121-91-5 

78-79-5 

67-63-0 

463-51-4' 

123-01-3 

142-72-3 

108-31-6 

108-76-1 

141-79-7 

128-98-7 

67-56-1 

74-89-5 

25376-45-8 

74-87-3 

75-09-2 

78-93-3 

74-88-4 

108-10-1 

40 CFR Ch. I (7-1-91 Edition) 

Chemical name 

Methyl methacrylate 

2-Methytpentane 

1 -Methyl-2.pyrrolidone... 

Methyl tert-butyl ether... 

Naphthalene 

Nit 

1-N 

Nonyl alcohol.. 

Nonytphenol... 

Nonyrphenoi. ethoxylated.. 

Octene 

Oil-soluble petroleum sulfonate, calcium salt.. 

OH-soluble petroleum sulfonate, sodium salt... 

Pentaerythrrtol 

n-Pentane 

3-Pentenenrtrlle 

Pentenes, mixed.. 

Perchloroethylene 

Phenol. 

1-Phenytethyl hydroperoxide.. 

Phorrvtpropane 

Phosgene 

Phthalic anhydride 

Propane 

Propionaldahyde 

Propionic add 

Propyl alcohol 

Propylene.. 

Propylene chlorohydrln.. 

Propylene glycolPropylene oxide 

Sodium cyanide 

Sorbitol 

Styrene 

Terephtharteadd.. 

1,1A2-Tel 

Tetraethyl lead.. 

Tetrahydrofuran... 

Terra (methyl-ethyl) lead... 

Tetramethyl lead 

Toluene.. 

Toruene-2,4-dramtne 

Totuene-2,44and, 2.6Hfisocyanate (80/20 

mixture) 

Tribrornomethane 

1.1.1 

1,1.2-Trlchloroethane.. 

Trichloroethylene 

Tricrriorottuoromethano.. 

1.1 _2-Trichloro-1,2,2-trtrluoroetharie... 

Triethanolamine. 

Triethylene glycol 

Vinyl acetate 

Vinyl chloride.. 

Vlnyedene dtrorlde... 

m-Xylene 

o-Xylene 

p-Xylene 

Xylenes (mixed) 

m-Xylenol 

CAS No.* 

80-62-6 

107-83-5 

872-50-4 

91-20-3 

98-95-3 

27215-95-8 

143-08-08 

25154-52-3 

9018-45-9 

25377-83-7 

115-77-5 

109-66-0 

4635-87-4 

109-67-1 

127-18-4 

108-95-2 

3071-32-7 

103-65-1 

75-44-5 

85-44-9 

74-88-6 

123-38-8 

79-09-4 

71-23-8 

115-07-1 

78-69-7 

57-55-6 

75-66-9 

143-33-9 

50-70-4 

100-42-5 

100-21-0 

79-34-5 

78-00-2 

10 

75-74-1 

108-68-3 

95-80-7 

26471-62-5 

75-25-2 

71-55-6 

79-00-5 

79-01-6 

75-69-4 

76-13-1 

102-71-6 

112-27-6 

108-05-4 

75-01-4 

75-35-4 

108-38-3 

95-47-6 

106-42-3 

1330-20-7 

576-26-1 

* CAS numbers refer to the Chemical Abstracts Registry 

numbers assigned to spsdflc chemicals. Isomers, or mixtures 

of chemrcafs. Some isomers or mixtures that are covered by 

the standards do not have CAS numbers assigned to them. 

The standards apply to all of the chemicals feed, whether 

CAS numbers have been assigned or not 

§ 60.668 Delegation of authority, 

(a) In delegating implementation 

and enforcement authority to a State 

632 

Environmental Protection Agency 

under i 111(c) of the Act, the authorities contained in paragraph (b) of this 

section shall be retained by the Administrator and not transferred to a 

State. 

(b) Authorities which will not be delegated to States: S 60.663(e). 

Subpart OOO—Standards of Performanco for Nonmotallic Mineral Processing Plants 

SOURCE 51 FR 31337, Aug. 1, 1985, unless 

otherwise noted. 

B 60.670 Applicability and designation of 

affected facility. 

(a) Except as provided in paragraphs 

(b), (c) and (d) of this section, the provisions of this subpart are applicable 

to the following affected facilities in 

fixed or portable nonmetailic mineral 

processing plants: each crusher, grinding mill, screening operation, bucket 

elevator, belt conveyor, bagging operation, storage bin, enclosed truck or 

rallcar loading station. 

(b) An affected facility that is subject to the provisions of subpart F or I 

or that follows in the plant process 

any facility subject to the provisions 

of subparts F or I of this part Is not 

subject to the provisions of this subpart. 

(c) Facilities at the following plants 

are not subject to the provisions of 

this subpart: 

(1) Fixed sand and gravel plants and 

crushed stone plants with capacities, 

as defined in $60,671, of 23 megagrams per hour (25 tons per hour) or 

less; 

(2) Portable sand and gravel plants 

and crushed stone plants with capacities, as defined in $ 60.671, of 136 megagrams per hour (150 tons per hour) 

or less; and 

(3) Common clay plants and pumice 

plants with capacities, as defined in 

$ 60.671, of 9 megagrams per hour (10 

tons per hour) or less. 

(d)(1) When an existing facility is replaced by a piece of equipment of 

equal or smaller size, as defined in 

$ 60.671, having the same function as 

the existing facility, the new facility is 

exempt from the provisions of 

$$ 60.672. 60.674, and 60.675 except as 

§ 60.671 

provided for in paragraph (d)(3) of 

this section. 

(2) An owner or operator seeking to 

comply with this paragraph shall 

comply with the reporting requirements of S 60.676 (a) and (b). 

(3) An owner or operator replacing 

all existing facilities in a production 

line with new facilities does not qualify for the exemption described in 

paragraph (d)(1) of this section and 

must comply with the provisions of 

$$ 60.672, 60.674 and 60.675. 

(e) An affected facility under paragraph (a) of this section that commences construction, reconstruction, 

or modification after August 31, 1983 

is subject to the requirements of this 

part. 

§ 60.671 Definitions. 

All terms used in this subpart, but 

not specifically defined in this section, 

shall have the meaning given them in 

the Act and in subpart A of this part. 

Bagging operation means the mechanical process by which bags are 

filled with nonmetailic minerals. 

Belt conveyor means a conveying 

device that transports material from 

one location to another by means of 

an endless belt that is carried on a 

series of idlers and routed around a 

pulley at each end. 

Bucket elevator means a conveying 

device of nonmetailic minerals consisting of a head and foot assembly which 

supports and drives an endless single 

or double strand chain or belt to 

which buckets are attached. 

Building means any frame structure 

with a roof. 

Capacity means the cumulative 

rated capacity of all initial crushers 

that are part of the plant. 

Capture system means the equipment (including enclosures, hoods, 

ducts, fans, dampers, etc.) used to capture and transport particulate matter 

generated by one or more process operations to a control device. 

Control device means the air pollution control equipment used to reduce 

particulate matter emissions released 

to the atmosphere from one or more 

process operations at a nonmetailic 

mineral processing plant. 

633 

* v 

si .n 

* * 

• V -'• 

*H 

" » i ; 

M «(. ••* -: 

* ) 

:\ '.