Current through Register Vol. 50, No. 9, September 20, 2024
A.
Applicability
1. The provisions of this
Subchapter apply to any vent stream discharging to the atmosphere and
originating from a process unit in which a reactor process or distillation
operation is located. This Subchapter shall apply to all vents located at
facilities that emit, or have the potential to emit, 25 tons per year (TPY) or
more of volatile organic compounds (VOC), plantwide, in the affected parishes
of Ascension, East Baton Rouge, Iberville, Livingston, and West Baton Rouge, or
50 TPY or more of VOC in the parishes of Calcasieu and Pointe Coupee. Once an
operation is considered to be covered by this Subchapter, it shall be so
considered ad infinitum. A decision tree is provided (Figure 1) to facilitate
determination of applicability to this Subchapter on a per vent basis. The
total resource effectiveness (TRE) index value may be applied on an individual
process vent stream basis for a given process unit. Compliance with this rule
shall be attained within a period of two years after promulgation. A facility
that has become subject to this regulation as a result of a revision of the
regulation shall comply with the requirements of this Section as soon as
practicable, but in no event later than one year from the promulgation of the
regulation revision. Any emission source that is subject to this rule and to
the Waste Gas Disposal Rule (LAC 33:III.2115) shall comply with this rule only.
This rule shall apply only to Standard Industrial Major Code 28.
2. Exemptions from the provisions of this
Subchapter are as follows:
a. any reactor
process or distillation vent stream for which an existing combustion device is
employed to control volatile organic compound (VOC) emissions is not required
to meet the 98 percent destruction or 20 parts per million (ppm) by volume
emissions limit until the combustion device is replaced for other
reasons;
b. any reactor process or
distillation operation that is designed and operated in a batch mode is not
subject to the provisions of this Subchapter;
c. any reactor process or distillation
operation that is part of a polymer manufacturing operation is not subject to
the provisions of this Subchapter;
d. any reactor process or distillation
operation operating in a process unit with a total design capacity of less than
1 gigagrams per year for all chemicals produced within that unit is not subject
to the provisions of this Subchapter except for the reporting and recordkeeping
requirements listed in Paragraph F.4 of this Section;
e. any vent stream for a reactor process or
distillation operation with a flow rate of less than 0.011 standard cubic
meters per minute or a total VOC concentration of less than 500 ppm by volume
is not subject to the provisions of this Subchapter except for the performance
testing requirements listed in Subparagraph D.3.b and Paragraph D.9 of this
Section and the reporting and recordkeeping requirements listed in Paragraph
F.3 of this Section;
f. any reactor
process or distillation operation which does not use, contain or produce VOCs
is not subject to the provisions of this Subchapter; and
g. any reactor process or distillation
operation that is subject to the Hazardous Organic NESHAP (HON), the NSPS of
Subchapter NNN for distillation operations or the NSPS of Subchapter RRR for
reactor processes is not subject to the provisions of this
Subchapter.
B. Definitions. Unless specifically defined
in LAC 33:III.111, the terms in this Subchapter shall have the meanings
commonly used in the field of air pollution control. Additionally, the
following meanings apply, unless the context clearly indicates
otherwise.
Batch Mode- a discontinuous process
involving the bulk movement of material through sequential manufacturing steps.
Mass, temperature, concentration and other properties of the system vary with
time. Batch processes are typically characterized as "nonsteady-state."
Boiler- any enclosed combustion device
that extracts useful energy in the form of steam.
By Compound- by individual stream
components, not carbon equivalents.
Continuous Recorder- a data recording
device that either records an instantaneous data value at least once every 15
minutes or records 15-minute or more frequent block average values.
Distillation Operation- an operation
separating one or more feed streams into two or more exit streams, 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 phases as they approach equilibrium within the
distillation unit.
Distillation Unit- 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- the portion of the combustion
chamber in a boiler occupied by the flame envelope.
Flow Indicator- a device that indicates
whether gas flow is present in a vent stream.
Halogenated Vent Stream- any vent stream
containing a total concentration of halogen atoms (by volume) contained in
halogenated organic compounds of 200 ppm by volume or greater determined by
using Method 18 (40 CFR Part 60, Appendix A, as incorporated by reference at
LAC 33:III.3003) or other test or validated data by the United States
Environmental Protection Agency's (EPA) Method 301 of 40 CFR Part 63, Appendix
A, or by engineering assessment or process knowledge that no halogenated
organic compounds are present. For example, 150 ppm by volume of ethylene
dichloride would contain 300 ppm by volume of total halogen atoms.
Incinerator- any enclosed combustion
device that is used for destroying organic compounds. Auxiliary fuel may be
used to heat waste gas to combustion temperatures. Any energy recovery section
present is not physically formed into one section; rather, the energy recovery
system is a separate section following the combustion section and the two are
joined by ducting or connections that carry flue gas.
Primary Fuel- the fuel that provides the
principal heat input to the device. To be considered primary, the fuel must be
able to sustain operation without the addition of other fuels.
Process Heater- 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- equipment assembled and
connected by pipes or ducts to produce, as intermediates or final products, one
or more synthetic organic chemical manufacturing industry (SOCMI) chemicals
(see LAC 33:III.2199.Appendix A). A process unit can operate independently if
supplied with sufficient feed or raw materials and sufficient storage
facilities.
Product- any compound or SOCMI chemical
that is produced as that chemical for sale as a product, by-product, co-product
or intermediate or for use in the production of other chemicals or
compounds.
Reactor Processes- unit operations in
which one or more chemicals or reactants other than air are combined or
decomposed in such a way that their molecular structures are altered and one or
more new organic compounds are formed.
Recovery Device- an individual unit of
equipment, such as an absorber, carbon adsorber, or condenser, capable of and
used for the purpose of recovering chemicals for subsequent use, reuse,
destruction, disposal by underground injection, or sale.
Recovery System- an individual recovery
device or series of such devices applied to one vent stream.
Total Organic Compounds (TOC)- those
compounds measured according to the procedures of Method 18 (40 CFR Part 60,
Appendix A, as incorporated by reference at LAC 33:III.3003), for the purpose
of measuring molar composition as required in Subparagraph D.5.b of this
Section, hourly emission rate as required in Paragraph D.2 and Subparagraph
D.5.d of this Section, and TOC concentration as required in Subparagraph F.1.d
and Paragraph F.2 of this Section. The definition of TOC excludes those
compounds that the administrative authority* designates as having negligible
photochemical reactivity as listed in
40
CFR 51.100(s).
Total Resource Effectiveness (TRE) Index
Value- a measure of the supplemental total resource requirement per
unit reduction of TOC associated with a process vent stream, based on vent
stream flow rate, emission rate of VOC, net heating value, and corrosion
properties (whether or not the vent stream contains halogenated compounds) as
quantified by the given equations. The TRE index is a decision tool used to
determine if the annual cost of controlling a given vent stream is acceptable
when considering the emissions reduction achieved.
Vent Stream- any gas stream discharged
directly from a distillation operation or reactor process to the atmosphere or
indirectly to the atmosphere after diversion through other process equipment.
The vent stream excludes relief valve discharges, equipment leaks including,
but not limited to, pumps, compressors, and valves, vents from storage vessels,
vents from transfer/loading operations, and vents from wastewater. The vent
stream also excludes process gaseous streams that are used as primary fuels.
The lines that transfer such fuels to a plant fuel gas system are not
considered vents.
Volatile Organic Compound Control Device-
any equipment used for oxidizing or destroying VOCs. Such equipment includes,
but is not limited to, incinerators, flares, boilers, and process
heaters.
C. Control Requirements
1. For individual vent streams from an
affected reactor process or distillation operation with a TRE index value less
than or equal to 1.0, the owner or operator shall:
a. reduce emission of TOC (less methane and
ethane) by 98 weight-percent or to a concentration of 20 ppm by volume, on a
dry basis corrected to three percent oxygen, whichever is less stringent by
means of a VOC recovery and/or control device, if such a control device is
necessary. If a boiler or process heater is used to comply with this Section,
then the vent stream shall be introduced into the flame zone of the boiler or
process heater; or
b. combust
emissions in a flare. Flares used to comply with this Section shall comply with
the requirements of
40 CFR
60.18. The flare operation requirement does
not apply if a process vents an emergency relief discharge into a common flare
header and causes the flare servicing the process to be out of compliance with
one or more of the provisions of the flare operation rule.
2. For each individual vent stream from an
affected reactor process or distillation operation with a TRE index value
greater than 1.0, the owner or operator shall maintain vent stream parameters
that result in a calculated TRE index value greater than 1.0 without the use of
a volatile organic compound control device and with or without the use of one
or more recovery devices. The TRE index shall be calculated at the outlet of
the final recovery device, if any, as specified in Clause D.5.a.i of this
Section except if an affected vent stream is mixed with an unaffected vent
stream prior to the final recovery device as specified in Paragraph D.5 of this
Section. If it can be demonstrated that a TRE index value is greater than 1.0
prior to the use of a recovery device, then such recovery device is not subject
to the requirements of this Subchapter.
D. Total Effectiveness Determination,
Performance Testing, and Exemption Testing
1.
For the purpose of demonstrating compliance with the TRE index value in
Paragraph C.2 of this Section, engineering assessment may be used to determine
process vent stream flow rate, net heating value, and TOC emission rate for the
representative operating condition expected to yield the lowest TRE index
value.
a. If the TRE value calculated using
such engineering assessment and the TRE equation in Paragraph D.6 of this
Section is greater than 4.0, then it is not required that the owner or operator
perform the measures specified in Paragraph D.5, the monitoring requirements in
Subsection E, or the reporting/record keeping requirements of Paragraph F.1 of
this Section. If a subsequent process change effects a reduction in the TRE
index value to 4.0 or less, the owner or operator is immediately subject to all
requirements of this Section that are applicable to a recalculated TRE value of
4.0 or less.
b. If the TRE value
calculated using such engineering assessment and the TRE equation in Paragraph
D.6 of this Section is less than or equal to 4.0, then it is required that the
owner or operator perform the measurements specified in Paragraph D.5 of this
Section.
c. Engineering assessment
includes, but is not limited to, the following:
i. previous test results that proved the test
was representative of current operating practices at the process
unit;
ii. bench-scale or
pilot-scale test data representative of the process under representative
operating conditions;
iii. maximum
flow rate specified or implied within a permit limit applicable to the process
vent;
iv. design analysis based on
accepted chemical engineering principles, measured process parameters, or
physical or chemical laws or properties. Examples for analytical methods
include, but are not limited to:
(a). use of
material balances based on process stoichiometry to estimate maximum VOC
concentrations;
(b). estimation of
maximum flow rate based on physical equipment design such as pump or blower
capacities;
(c). estimation of TOC
concentrations based on saturation conditions; or
(d). estimation of maximum expected net
heating value based on the stream concentration of each organic compound or,
alternatively, as if all TOC in the stream were the compound with the highest
heating value; and
v.
documentation of all data, assumptions, and procedures used in the engineering
assessment.
2. For purposes of demonstrating compliance
with the control requirements of this Subchapter, the process unit shall be run
at representative operating conditions and flow rates during any performance
test.
3. The following methods in
40 CFR Part 60, Appendix A, as incorporated by reference in LAC 33:III.Chapter
30, shall be used to demonstrate compliance with the emission limit or percent
reduction efficiency requirement listed in Subparagraph C.1.a of this Section.
a. Method 1 (40 CFR Part 60, Appendix A, as
incorporated by reference at LAC 33:III.3003) or Method 1A (40 CFR Part 60,
Appendix A, as incorporated by reference at LAC 33:III.3003), as appropriate,
shall be used 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 located after the last
recovery device but prior to the inlet of the control device, prior to any
dilution of the process vent stream, and prior to release to the
atmosphere.
b. Method 2 ( 40 CFR
Part 60, Appendix A, as incorporated by reference at LAC 33:III.3003), Method
2A (40 CFR Part 60, Appendix A, as incorporated by reference at LAC
33:III.3003), Method 2C (40 CFR Part 60, Appendix A, as incorporated by
reference at LAC 33:III.3003), or Method 2D (40 CFR Part 60, Appendix A, as
incorporated by reference at LAC 33:III.3003), as appropriate, shall be used
for determination of the gas stream volumetric flow rate.
c. The emission rate correction factor,
integrated sampling and analysis procedure of Method 3 (40 CFR Part 60,
Appendix A, as incorporated by reference at LAC 33:III.3003) shall be used to
determine the oxygen concentration (%O2d) for the
purpose of determining compliance with the 20 ppm by volume limit. The sampling
site shall be the same as that for the TOC samples, and samples shall be taken
during the same time that the TOC samples are taken. The TOC concentration
corrected to 3 percent oxygen (Cc) shall be computed
using the following equation.
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Cc = concentration of TOC (minus
methane and ethane) corrected to 3 percent O2, dry
basis, ppm by volume
CTOC = concentration of TOC (minus
methane and ethane), dry basis, ppm by volume
% O2d = concentration of oxygen,
dry basis, percent by volume
d. Method 18 (40 CFR Part 60, Appendix A, as
incorporated by reference at LAC 33:III.3003) shall be used to determine the
concentration of TOC (minus methane and ethane) at the outlet of the control
device when determining compliance with the 20 ppm by volume limit, or at both
the control device inlet and outlet when the reduction efficiency of the
control device is to be determined.
i. The
minimum sampling time for each run shall be one 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.
ii. The emission reduction (R) of TOC (minus
methane and ethane) shall be determined using the following equation.
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R = emission reduction, percent by weight
Ei = mass rate of TOC (minus
methane and ethane) entering the control device, kilogram TOC per hour
Eo = mass rate of TOC (minus
methane and ethane) discharged to the atmosphere, kilogram TOC per hour
iii. The mass rates of TOC
(Ei, Eo) shall be computed using
the following equations.
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where:
Cij, Coj =
concentration of sample component "j" of the gas stream at the inlet and outlet
of the control device, respectively, dry basis, ppm by volume
Mij, Moj =
molecular weight of sample component "j" of the gas stream at the inlet and
outlet of the control device, respectively, grams per gram-mole
Qi, Qo =
flow rate of gas at the inlet and outlet of the control device, respectively,
dry standard cubic meters per minute
K2 = 2.494 x 10-6 (liters per
minute)(gram-mole per standard cubic meter) is 20°C
iv. The TOC concentration
(CTOC) is the sum of the individual components and shall
be computed for each run using the following equation.
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CTOC = concentration of TOC (minus
methane and ethane), dry basis, ppm by volume
Cj = concentration of sample
component "j", dry basis, ppm by volume
n = number of components in the sample
e. When a boiler or process heater
with a design heat input capacity of 44 megawatts or greater, or a boiler or
process heater into which the process stream is introduced with the primary
fuel, is used to comply with the control requirements, an initial performance
test is not required.
4.
When a flare is used to comply with the control requirements of this
Subchapter, the flare shall comply with the requirements of
40 CFR
60.18, as incorporated by reference in LAC
33:III.Chapter 30.
5. The following
test methods shall be used to determine compliance with the TRE index value in
Paragraph C.2 of this Section.
a. Method 1 (
40 CFR Part 60, Appendix A, as incorporated by reference at LAC 33:III.3003) or
Method 1A (40 CFR Part 60, Appendix A, as incorporated by reference at LAC
33:III.3003), as appropriate, shall be used for selection of the sampling site.
i. The sampling site for the vent stream
molar composition determination and flow rate prescribed in Subparagraphs D.5.b
and c of this Section shall be, except for the situations outlined in Clause
D.5.a.ii of this Section, after the final recovery device, if a recovery system
is present, prior to any post-reactor or post-distillation unit introduction of
halogenated compounds into the process vent stream. No traverse site selection
method is needed for vents smaller than 10 centimeters in diameter.
ii. If any gas stream other than the reactor
or distillation vent stream is normally conducted through the final recovery
device:
(a). the sampling site for the vent
stream flow rate and molar composition shall be prior to the final recovery
device and prior to the point at which any nonreactor or nondistillation stream
or stream from a nonaffected reactor or distillation unit is introduced. Method
18 (40 CFR Part 60, Appendix A, as incorporated by reference at LAC
33:III.3003) shall be used to measure organic compound concentrations at this
site;
(b). the efficiency of the
final recovery device is determined by measuring the organic compound
concentrations using Method 18 (40 CFR Part 60, Appendix A, as incorporated by
reference at LAC 33:III.3003) at the inlet to the final recovery device after
the introduction of all vent streams and at the outlet of the final recovery
device;
(c). the efficiency of the
final recovery device according to Subclause D.5.a.ii.(b) of this Section shall
be applied to the organic compound concentrations measured according to
Subclause D.5.a.ii.(a) of this Section to determine the concentrations of
organic compounds from the final recovery device attributable to the reactor or
distillation vent stream. The resulting organic compound concentrations are
then used to perform the calculations outlined in Subparagraph D.5.d of this
Section.
b.
The molar composition of the vent stream shall be determined as follows.
i. Method 18 (40 CFR Part 60, Appendix A, as
incorporated by reference at LAC 33:III.3003) shall be used to measure the
concentration of organic compounds including those containing
halogens.
ii. ASTM D1946-77 shall
be used to measure the concentration of carbon monoxide and hydrogen.
iii. Method 4 (40 CFR Part 60, Appendix A, as
incorporated by reference at LAC 33:III.3003) shall be used to measure the
content of water vapor.
c. The volumetric flow rate shall be
determined using Method 2, Method 2A, Method 2C or Method 2D of 40 CFR Part 60,
Appendix A, as incorporated by reference at LAC 33:III.3003, as
appropriate.
d. The emission rate
of TOC (minus methane and ethane) (ETOC) in the vent
stream shall be calculated using the following equation.
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where:
ETOC = emission rate of TOC (minus
methane and ethane) in the sample, kilograms per hour
K2 = constant, 2.494 x 10-6 (liters
per ppm) x (gram-moles per standard cubic meter [scm]) (kilograms per gram)
(minutes per hour), where standard temperature for (gram-mole per scm) x
(gram-mole per scm) is 20°C
Cj = concentration of sample
component "j", on a dry basis, in ppm as measured by Method 18 (40 CFR Part 60,
Appendix A, as incorporated by reference at LAC 33:III.3003), as indicated in
Subparagraph D.3.d of this Section
Mj = molecular weight of sample
component "j", grams per gram-mole
Qs = vent stream flow rate (scm per
minute) at a temperature of 20°C, on a dry basis
e. The total process vent stream
concentration (by volume) of compounds containing halogens (ppm by volume, by
compound) shall be summed from the individual concentrations of compounds
containing halogens which were measured by Method 18 (40 CFR Part 60, Appendix
A, as incorporated by reference at LAC 33:III.3003).
f. The net heating value of the vent stream
shall be calculated using the equation.
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HT = net heating value of the
sample (megajoules per standard cubic meter), where the net enthalpy per mole
of vent stream is based on combustion at 25°C and 760 millimeters of mercury,
but the standard temperature for determining the volume corresponding to one
mole is 20°C, as in the definition of Qs (vent stream
flow rate)
K1 = constant, 1.740 x 10-7 (ppm)-1
(gram-mole per standard cubic meter), (megajoules per kilocalorie), where
standard temperature for (gram-mole per standard cubic meter) is 20°C
Bws = water vapor content of the
vent stream, proportion by volume; except that if the vent stream passes
through a final stream jet and is not condensed, it shall be assumed that Bws =
0.023 in order to correct 2.3 percent moisture
Cj = concentration on a dry basis
of sample component "j" in parts per million, as measured for all organic
compounds by Method 18 (40 CFR Part 60, Appendix A, as incorporated by
reference at LAC 33:III.3003) and measured for hydrogen and carbon monoxide by
ASTM D1946-77
Hj = net heat of combustion of
sample component "j", kilocalories per gram-mole, based on combustion at 25°C
and 760 millimeters of mercury. The heats of combustion of vent stream
components shall be determined using ASTM D2382-76 if published values are not
available or cannot be calculated.
6. The TRE index value of the vent shall be
calculated using the following equation.
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where:
TRE = TRE index value
ETOC = hourly emission rate of TOC
(minus methane and ethane), kilograms per hour, as calculated in Subparagraph
D.5.d of this Section
Qs = vent stream flow rate standard
cubic meters per minute at a standard temperature of 20°C
HT = vent stream net heating value
(megajoules per standard cubic meter), as calculated in Subparagraph D.5.f of
this Section
a, b, c, d = coefficients presented in Table 1.
|
Table 1
|
|
Type of Stream
|
Control Device Basis
|
Values of Coefficient
|
|
|
|
a
|
b
|
c
|
d
|
|
Nonhalogenated
|
Flare
|
2.129
|
0.183
|
-0.005
|
0.359
|
|
|
Thermal incinerator 0 percent heat recovery
|
3.075
|
0.021
|
-0.037
|
0.018
|
|
|
Thermal incinerator 70 percent heat recovery
|
3.803
|
0.032
|
-0.042
|
0.007
|
|
Halogenated
|
Thermal incinerator and scrubber
|
5.470
|
0.181
|
-0.040
|
0.004
|
a. The owner
or operator of a unit with a nonhalogenated vent stream shall use the
applicable coefficients in Table 1 to calculate the TRE index value based on a
flare, thermal incinerator with 0 percent heat recovery, and a thermal
incinerator with 70 percent heat recovery, and shall select the lowest TRE
index value.
b. The owner or
operator of a unit with a halogenated vent stream, determined as any stream
with a total concentration of halogen atoms contained in organic compounds of
200 ppm by volume or greater, shall use the applicable coefficients in Table 1
to calculate the TRE index value based on a thermal incinerator and
scrubber.
7. Each owner
or operator of a vent stream subject to Paragraph C.2 of this Section shall
recalculate the flow rate, TOC concentration, and TRE index value for that vent
stream within two weeks of any process change that could effect a change in one
or more of these vent stream parameters. The recalculations must be made using
the methods and procedures contained in this Subsection. Examples of process
changes include, but are not limited to, changes in production capacity,
feedstock type, or catalyst type or replacement, removal, or addition of
recovery equipment.
8. Where a TRE
index value, recalculated as required in Paragraph D.7 of this Section, yields
a value less than or equal to 1.0, the owner or operator shall, within one week
of the recalculation, notify the administrative authority* of the process
change and the results of the recalculation and shall conduct a performance
test, as provided in Subparagraph D.1.b and Paragraph D.5 of this Section, as
soon as possible, but no later than 90 days after the recalculation. If the
recalculated TRE index value is verified by the performance test to be less
than or equal to 1.0, the owner or operator is immediately subject to all
requirements of this Section that are applicable to a recalculated TRE value of
1.0 or less.
9. Procedures
contained in Subparagraphs D.9.a-e of this Section shall be used to demonstrate
that a process vent stream has a VOC concentration below 500 ppm by volume.
a. The sampling site shall be selected as
specified in Subparagraph D.3.a of this Section.
b. Method 18 (40 CFR Part 60, Appendix A, as
incorporated by reference at LAC 33:III.3003) or Method 25A (40 CFR Part 60,
Appendix A, as incorporated by reference at LAC 33:III.3003) shall be used to
measure concentration; alternatively, any other method or data that has been
validated according to the protocol in EPA Method 301 of 40 CFR Part 63,
Appendix A may be used.
c. Where
Method 18 (40 CFR Part 60, Appendix A, as incorporated by reference at LAC
33:III.3003) is used, the following procedures shall be used to calculate parts
per million by volume concentration.
i. The
minimum sampling time for each run shall be one 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 approximately equal intervals in time,
such as 15-minute intervals during the run.
ii. The concentration of TOC (minus methane
and ethane) shall be calculated using Method 18 (40 CFR Part 60, Appendix A, as
incorporated by reference at LAC 33:III.3003) according to Subparagraph D.3.d
of this Section.
d.
Where Method 25A (40 CFR Part 60, Appendix A, as incorporated by reference at
LAC 33:III.3003) is used, the following procedures shall be used to calculate
parts per million by volume TOC concentration.
i. Method 25A (40 CFR Part 60, Appendix A, as
incorporated by reference at LAC 33:III.3003) shall be used only if a single
VOC is greater than 50 percent of total VOC, by volume, in the process vent
stream.
ii. The process vent stream
composition may be determined by either process knowledge, test data collected
using an appropriate method previously promulgated, or a method of data
collection validated according to the protocol in EPA Method 301 of 40 CFR Part
63, Appendix A. Examples of information that could constitute process knowledge
include calculations based on material balances, process stoichiometry, or
previous test results provided the results are still relevant to the current
process vent stream conditions.
iii. The VOC used as the calibration gas for
Method 25A (40 CFR Part 60, Appendix A, as incorporated by reference at LAC
33:III.3003) shall be the single VOC present at greater than 50 percent of the
total VOC by volume.
iv. The span
value for Method 25A (40 CFR Part 60, Appendix A, as incorporated by reference
at LAC 33:III.3003) shall be 50 ppm by volume.
v. Use of Method 25A (40 CFR Part 60,
Appendix A, as incorporated by reference at LAC 33:III.3003) 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.
vi. The concentration of TOC shall be
corrected to 3 percent oxygen using the procedures and equation in Subparagraph
D.3.c of this Section.
e. The owner or operator shall demonstrate
that the concentration of TOC including methane and ethane measured by Method
25A (40 CFR Part 60, Appendix A, as incorporated by reference at LAC
33:III.3003) is below 250 ppm by volume with VOC concentration below 500 ppm by
volume to qualify for the low concentration exclusion.
E. Monitoring Requirements
1. The owner or operator of an affected
facility that uses an incinerator to seek to comply with the TOC emission limit
specified under Subparagraph C.1.a of this Section shall install, calibrate,
maintain, and operate according to manufacturer's specifications, a temperature
monitoring device equipped with a continuous recorder having an accuracy of
+-0.5°C, or alternatively +-1 percent, as follows.
a. Where an incinerator other than a
catalytic incinerator is used, a temperature monitoring device shall be
installed in the firebox or in the ductwork immediately downstream of the
firebox before any substantial heat exchange is encountered.
b. Where a catalytic incinerator is used,
temperature monitoring devices shall be installed in the gas stream immediately
before and after the catalyst bed.
2. The owner or operator of an affected
facility that uses a flare to seek to comply with Subparagraph C.1.b of this
Section shall install, calibrate, maintain, and operate according to
manufacturer's specifications, a heat-sensing device, such as an ultraviolet
beam sensor or thermocouple, at the pilot light to indicate the continuous
presence of a flame.
3. The owner
or operator of an affected facility that uses a boiler or process heater with a
design heat input capacity less than 44 megawatts to seek to comply with
Subparagraph C.1.b of this Section shall install, calibrate, maintain, and
operate according to the manufacturer's specifications, a temperature
monitoring device in the firebox or in the ductwork immediately downstream of
the firebox before any substantial heat exchange is encountered. The monitoring
device should be equipped with a continuous recorder and have an accuracy of
+-1 percent of the temperature being measured expressed in degrees Celsius or
+-0.5°C, whichever is greater. Any boiler or process heater in which all vent
streams are introduced with primary fuel is exempt from this
requirement.
4. The owner or
operator of an affected facility that seeks to demonstrate compliance with the
TRE index limit specified under Paragraph C.2 of this Section shall install,
calibrate, maintain, and operate according to manufacturer's specifications the
following equipment:
a. where an absorber is
the final recovery device in the recovery system:
i. a scrubbing liquid temperature monitor
equipped with a continuous recorder; and
ii. a specific gravity monitor equipped with
continuous recorders;
b.
where a condenser is the final recovery device in the recovery system, 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;
c. where a carbon adsorber
is the final recovery device unit in the recovery system, an integrating
regeneration stream flow monitoring device having an accuracy of +-10 percent,
capable of recording the total regeneration stream mass flow for each
regeneration cycle, and a carbon bed temperature monitoring device having an
accuracy of +-1 percent of the temperature being monitored, or +-0.5°C, capable
of recording the carbon bed temperature after each regeneration and within 25
minutes of completing any cooling cycle;
d. where a pressure swing adsorption (PSA)
unit is the final recovery device in the recovery system, instead of
Subparagraph E.4.c of this Section the temperature of the bed near the inlet
and near the outlet shall be continuously monitored and recorded. The
temperature monitoring devices shall have an accuracy of +-1 percent of the
temperature being measured or +-0.5°C. Proper operation shall be evidenced by a
uniform pattern of temperature increases and decreases near the inlet and a
fairly constant temperature near the outlet;
e. where an absorber scrubs halogenated
streams after an incinerator, boiler, or process heater, the following
monitoring equipment is required for the scrubber:
i. a pH monitoring device equipped with a
continuous recorder; and
ii. flow
meters equipped with continuous recorders to be located at the scrubber
influent for liquid flow and the scrubber inlet for gas stream flow;
f. as noted in Clause F.1.d.iv of
this Section an organics monitoring device may be used as an alternative
method.
5. The owner or
operator of a process vent using a vent system that contains bypass lines
(other than low leg drains, high point bleeds, analyzer vents open-ended valves
or lines and pressure relief valves) that could divert a vent stream away from
the combustion device used shall either:
a.
install, calibrate, maintain, and operate a flow indicator/recorder that
provides a record of vent stream flow at least once every 15 minutes. The flow
indicator shall be installed at the entrance to any bypass line that diverts
the vent stream away from the combustion device to the atmosphere; or
b. secure the bypass line valve in the closed
position with a car-seal or a lock-and-key type configuration. A visual
inspection of the seal or closure mechanism shall be performed at least once
per month to ensure that the valve is maintained in the closed position and the
vent stream is not diverted through the bypass line.
F. Reporting/Recordkeeping
Requirements
1. Each reactor process or
distillation operation subject to this Subchapter shall keep records of the
following parameters measured during a performance test or TRE determination
required under Subsection D of this Section and required to be monitored under
Subsection E of this Section:
a. where an
owner or operator subject to the provisions of this Subchapter seeks to
demonstrate compliance with Subparagraph C.1.a of this Section through the 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 period as the performance testing; and
ii. the percent reduction of TOC determined
as specified in Paragraph D.3 of this Section achieved by the incinerator or
concentration of TOC (parts per million by volume, by compound) determined as
specified in Paragraph D.3 of this Section at the outlet of the control device
on a dry basis corrected to 3 percent oxygen;
b. where an owner or operator subject to the
provisions of this Subchapter seeks to demonstrate compliance with Subparagraph
C.1.a of this Section through the 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
megawatts measured at least every 15 minutes and averaged over the same time
period as the performance testing;
iii. any boiler or process heater in which
all vent streams are introduced with primary fuel are exempt from these
requirements;
c. where
an owner or operator subject to the provisions of this Subchapter seeks to
demonstrate compliance with Subparagraph C.1.b of this Section through use of a
smokeless flare, flare design (i.e., steam-assisted, air-assisted, or
nonassisted), all visible emission readings, heat content determinations, flow
measurements, and exit velocity determinations made during the performance
test; continuous flare pilot flame monitoring, and all periods of operation
during which the pilot flame is absent;
d. where an owner or operator subject to the
provisions of this Subchapter seeks to demonstrate compliance with Paragraph
C.2 of this Section:
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, if approved by the administrative authority*) and average exit
temperature of the absorbing liquid measured at least every 15 minutes and
averaged over the same time period as 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 as
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 stream
mass or volumetric flow measured at least every 15 minutes and averaged over
the same time period as 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 Clause
F.1.d.i, ii, or iii of this Section, 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 as the performance testing while the vent stream is
normally routed and constituted; and
v. all measurements and calculations
performed to determine the flow rate, volatile organic compound concentration,
heating value, and TRE index value of the vent stream;
vi. where a pressure swing adsorption (PSA)
unit is the final recovery device in the recovery system, the temperature of
the bed near the inlet and near the outlet shall be continuously monitored and
recorded. The temperature monitoring devices shall have an accuracy of +-0.5°C.
Proper operation shall be evidenced by a uniform pattern of temperature
increases and decreases near the inlet and a fairly constant temperature near
the outlet.
2. Each reactor process or distillation
operation seeking to comply with Paragraph C.2 of this Section shall also keep
records of the following information:
a. any
changes in production capacity, feedstock type, or catalyst type or of any
replacement, removal, and addition of recovery equipment or reactors and
distillation units;
b. any
recalculation of the flow rate, TOC concentration or TRE value performed
according to Paragraph D.7 of this Section.
3. Each reactor process or distillation
operation seeking to comply with the flow rate or concentration exemption level
in Subparagraph A.2.e of this Section shall keep records to indicate that the
stream flow is less than 0.011 standard cubic meters per minute or the
concentration is less than 500 ppm by volume.
4. Each reactor process or distillation
operation seeking to comply with the production capacity exemption level in
Subparagraph A.2.d of this Section of less than one gigagrams per year shall
keep records of the design production capacity or any changes in equipment or
process affected process unit. operation that may affect design production
capacity of the affected process unit.
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AUTHORITY NOTE:
Promulgated in accordance with
R.S.
30:2054.
