## State of Wisconsin

DEPARTMENT OF NATURAL RESOURCES 101 S. Webster Street Box 7921 Madison WI 53707·7921 Scott Walker, Governor Cathy Stepp, Secretary

Telephone 608-266-2621 Toll Free 1-888-936-7463 TTY Access via relay

- 711



### January 26, 2012

Ms. Susan Hedman Regional Administrator U.S. Environmental Protection Agency (EPA) 77 West Jackson Boulevard, R-19J Chicago IL 60604-3507

Subject: Revisions to Wisconsin's Ozone State Implementation Plan

Dear Ms. Hedman:

The Wisconsin Department of Natural Resources (WDNR) submitted a State Implementation Plan (SIP) revision on November 16,2011 regarding changes to cbs. NR 400,419,421,422,423,439, and 484, Wis. Adm. Code. The revised rules ensure that reasonably available control technology (RACT) for volatile organic compounds (VaC) is required in Wisconsin's moderate ozone nonattainment counties consistent with applicable U.S. EPA Control Techniques Guideline (CTG) documents. As correctly noted by u.S. EPA Region V staff, some of the rules submitted reference sections of ch. NR 440, Standards ofPerfonnance for New Stationary Sources, Wis. Adm. Code. As such, the purpose of this letter is to fonnally request inclusion of the referenced sections 

### (NR 440.67 

## 5,**440~** 

### 686, and 440.705, Wis. Adm. Code) into Wisconsin's Ozone SIP.

The WDNR has the legal authority under Wisconsin law to adopt and implement these requested SIP revisions. Section 285.11 (6), Wis. Stats., authorizes the WDNR to develop and revise the SIP for prevention, abatement, and control of air pollution. The WDNR conducted a public hearing on ch. NR 440, Wis. Adm. Code, on November 21, 2006. A copy of the public hearing notice is included as an attachment.

In accordance with the April 6, 2011 McCabe Memo, one paper-copy of the SIP revision documents are enclosed. 

### In addition, an electronic copy of these documents is provided as well on an enclosed CD. If you have any questions regarding this submittal, please feel free to call Joseph Hoch at 608-267-7543 or Ralph Patterson at 608-267-7546.



# Dt

Cathy St pp, Secretary 

# 'V Wisconsin Department**ofN~tural** 

### Resources

cc: Patrick Stevens

- 

### AD/8 William Baumann

- 

### AM/7 Joseph Hoch

- 

### AM/7 Ralph Patterson

- 

### AM/7 Cheryl Newton

- U.S. EPA Region V (A-18J), 77 West Jackson Boulevard, Chicago, IL 60604 Douglas Aburrano

- U.S. EPA Region V (AR-18J), 77 West Jackson Boulevard, Chicago, IL 60604 Jacqueline Nwia

- U.S. EPA Region V (AT-18J), 77 West Jackson Boulevard, Chicago, IL 60604

dnr.wLgov wisconsin.gov 

## Naturally 

# WISCONSIN () PRlNTED

"" ONRECYCLE.D

- - PAPER

## Summary of Attachments: Hard Copy and Electronic

Attachment 1 - Notice of Public Hearing for ch. NR 440, Wis. Adm. Code

Attachment 2 - Sections NR 440.675, 440.686, and 440.705, Wis. Adm. Code Page 2

### BEFORE THE DEPARATMENT OF·NATURAL RESOURCES

NOTICE OF PUBLIC HEARING AM-OS-06

NOTICE IS HEREBY GIVEN that pursuant to SSe 

### 227.11(2)(a), 285.11(1) and 285.27(1)(a), Stats., interpreting s. 285.11(1), Stats., the Department of Natural Resources will hold a public hearing on revisions to ch., NR 440, Wis. Adm. Code, relating to incorporation of revisions and additions to the federal New Source Performance Standards. Under section 111 of the Clean Air Act, the U.S. Environmental Protection Agency is required to promulgate regulations establishing standards of performance of new stationary

sources (NSPS). These standards are contained in 40 CFR Part 60. The Department is required, under s. 285.27(1 )(a), Stats., to incorporate these standards into rule, and does so in ch. NR 440. Periodically it is necessary to amend ch. NR 440 to address changes the EPA makes to existing NSPS and to incorporate standards promulgated by EPA for new source categories. These proposed reVisions address changes made by the EPA between July 1994 and April 2005 to general reqUirements which apply to all source categories, and to the specific standards for 60 individual source categories. Requirements relating to mercury emission from certain electric steam generating units which EPA promulgated on May 18, 2005 and subsequently amended are not proposed here. Those requirements will 

### be addressed separately in 

### Natural Resources Board Order No. AM-32-05. Standards for 5 source categories not currently included in ch. NR 440 are also being proposed.

NOTICE 'IS HEREBY FURTHER GIVEN that pursuant to s. 227.114, Stats., it is not anticipated that the proposed rule will have a substantial economic impact on small businesses. The proposed rules

are substantively identical to rules already in effect at the federal level. Any small businesses currently subject to the federal reqUirements will not be impacted by incorporation of these requirements into the Wisconsin Administrative Code. The Department's Small Business RegUlatory Coordinator may be contacted at SmatlBusiness@dnr.state.wLus or by calling (608) 266-1959.

NOTICE IS HEREBY FURTHER GIVEN that the Department has made a preliminary determination that this action does not involve significant adverse environmental effects and does not need an environmental analysis under ch. NR 150, Wis. Adm. Code. However, based on the comments received, the Department may prepare an environmental analysis before proceeding with the proposal. This environmental review document would summarize the Department's consideration of the impacts of the proposal and reasonable alternatives.

NOTICE IS HEREBY FURTHER GIVEN that the hearing will be held on:

November 21, 2006 Tuesday Room G09, GEF #2 Building, 101 South Webster Street, Madison at 1:00 p.m.

NOTICE IS HEREBY FURTHER GIVEN that pursuant to the Americans with Disabilities Act, reasonable accommodations, including the provision of information material in an alternative format, will be provided for qualified individuals with disabilities upon request. Please call Robert Eckdale at (608) 266-2856 or bye-mail at Robert.Eckdale@dnr.state.wLus with specific information on your request at least 10 days before the date of the scheduled hearing.

The proposed rule and supporting documents, including the fiscal estimate may be viewed and downloaded and comments electronically submitted at the follOWing Internet site: http://adminrules.wisconsin.gov. (Search this Web site using the Natural Resources Board Order number AM-05-06.) Written comments on the proposed rule may be submitted via U.S. mail to Mr. Robert Eckdale, Bureau of Air Management, P.O. Box 7921, Madison, WI 53707 or bye-mail to Robert.Eckdale@dnr.state.wi.us. Comments may be submitted until December 1,2006. Written comments whether submitted electronically or by U.S. mail will have the same weight and effect as oral

### statements presented at the pUblic hearings. If you do not have Internet access, a personal copy of the proposed rule and supporting documents, including the fiscal estimate may be obtained from Robert Eckdale, Bureau of Air Management, P.O. Box 7921, Madison, WI 532707' or by calling (608) 266-2856.

Dated at Madison, Wisconsin

# c:::z-~ 

# / 

# t**c:l~** cJ(/

STATE OF WISCONSIN DEPARTMENT OF NATURAL RESOURCES



## By Scott Hassett, Secretary420 NR 440.67 WISCONSIN ADMINISTRATIVE CODE

The Wisconsin Administrative Code on this web site is current through the last published Wisconsin Register . See also Are the Codes on this Website Official? 

### Register, May 2008, No. 629 equipment for mixing, filtering, blending and storage of the spinning solutions. (q) “Synthetic fiber” means any fiber composed partially or entirely of materials made by chemical synthesis or made partially or entirely from chemically−modified naturally−occurring materials. (r) “Viscose process” means the fiber forming process where cellulose and concentrated caustic soda are reacted to form soda or alkali cellulose. This reacts with carbondisulfide to form sodium cellulose xanthate which is then dissolved in a solution of caustic soda. The solution is spun into anacid coagulating bath after ripening. This precipitates thecellulose in the form of a regenerated cellulose filament. (3) S TANDARD FOR VOLATILE ORGANIC COMPOUNDS.On and after the date on which the initial performance test required to be conducted by s. NR 440.08 is completed, no owner or operator subject to the provisions of this section may cause the discharge into the atmosphere from any affected facility that produces acrylic fibers VOC emissions that exceed 10 kg/Mg (20 lb/ton)solvent feed to the spinning solution preparation system or precipitation bath. VOC emissions from affected facilities that produce both acrylic and nonacrylic fiber types may not exceed 10 kg/Mg (20 lb/ton) solvent feed. VOC emissions from affected facilities that produce only nonacrylic fiber types may not exceed 17 kg/Mg (34 lb/ton) solvent feed. Compliance with the emission limitations is determined on a 6−month rolling average basis as described in sub. (4). (4) P ERFORMANCE TEST AND COMPLIANCE PROVISIONS. (a) Section NR 440.08 (6)does not apply to the performance test procedures required by this section. (b) Each owner or operator of an affected facility shall determine compliance with the applicable standard in sub. (3)by determining and recording monthly the VOC emissions per unit

mass solvent feed from each affected facility for the current and preceding 5 consecutive calendar months and using these values to calculate the 6−month average emissions. Each calculation is considered a performance test. The owner or operator of an affected facility shall use the following procedure to determine VOC emissions for each calendar month:1. Install, calibrate, maintain, and operate monitoring devices that continuously measure and permanently record for each calendar month the amount of makeup solvent and solvent feed. These values shall be used in calculating VOC emissions according to subd. 2. All monitoring devices, meters and peripheral equipment shall be calibrated and any error recorded. T otal compounded er ror of the flow measuring and recording devicesmay not exceed 1% accuracy over the operating range. As an alternative to measuring solvent feed the owner or operator may: a. Measure the amount of recovered solvent returned to thesolvent feed storage tanks and use the following equation to determine the amount of solvent feed: Solvent Feed = Makeup Solvent + Recovered Solvent + Change in the Amount of Solvent Contained in the Solvent Feed Holding Tank. b. Measure and record the amount of polymer introduced into the af fected facility and the solvent−to−polymer ratio of the spinning solutions and use the following equation to determine the amount of solvent feed:

Solvent Feed 

##  n

i 1 (Polymer Used) i  (Solvent–to–Polymer Ratio) iwhere subscript “i” denotes each particular spinning solution used during the test period; values of “i” vary from one tothe total number of spinning solutions, “n,” used during the calendar month. 2. VOC emissions shall be determined each calendar month by use of the following equations: 

### DSMM where I−N− S M E PV W
W W 

### = =



## K DSS S PV

W 

## =

W SE 

## S I

− I I =

where all values are for the calendar month only and where: E is the VOC emissions in kg/Mg (lb/ton) solvent S Vis the measured or calculated volume of solvent feed in liters (gallons) S W is the weight of solvent feed in Mg (ton) MVis the measured volume of makeup solvent in liters (gallons) MW is the weight of makeup in kg (lb) N is the allowance for nongaseous losses, 13 kg/Mg (26 lb/ ton) solvent feed to the spinning solution preparation system and precipitation bath. This value shall be used in all cases unless anowner or operator demonstrates to the satisfaction of the department that greater nongaseous losses occur at the affected facility. In this case, the greater value may be substituted in the equation. S Pis the fraction of measured volume that is actual solvent (excludes water) D is the density of the solvent in kg/liter (lb/gallon) K is a conversion factor, 1000 kg/Mg (2,000 lb/ton) I is the allowance for solvent inventory variation or changes in the amount of solvent contained in the af fected facility, kg/Mg (lb/ton) solvent feed (may be positive or negative) I S is the amount of solvent contained in the af fected facility at the beginning of test period, as determined by the owner or operator, in kg (lb) IEis the amount of solvent contained in the af fected facilityat the close of the test period, as determined by the owner or operator, in kg (lb) (5) REPORTING REQUIREMENTS.(a) The owner or operator of an affected facility shall submit a written report to the department of the following: 1. The results of the initial performance test; and 2. The results of subsequent performance tests that indicate that VOC emissions exceed the standards in sub. (3) . These reports shall be submitted quarterly at 3−month intervals after the initial performance test. If no exceedances occur during a particular quarter, a report stating this shall be submitted to the department semiannually.(b) Solvent−spun synthetic fiber producing facilities exempted from these standards in sub. (1) (a)(those producing less than 500 Mg (551 tons) annually) shall report to the department within 30 days whenever extruded fiber for the preceding 12 calendar months exceeds 500 Mg (551 tons).

History: Cr. Register, September, 1986, No. 369 , eff. 10−1−86; renum. (2) (a) (intro.) and 1. to 18. to be (2) (intro.) and (a) to (r) and am. (2) (intro.), am. (3) (a), r. (5) (c), Register, September, 1990, No. 417 , eff. 10−1−90; am. (4) (b) 2. and (5) (a) 2., Register, July, 1993, No. 451 , eff. 8−1−93; CR 06−109 : am. (1) (a), (4) (b) (intro.) and (5) (b), renum. (3) (a) to be (3) and am., r. and recr. (4) (b) 2. Register May 2008 No. 629 , eff. 6−1−08.

NR 440.675 Volatile organic compound (VOC) emissions from the synthetic organic chemical manufacturing industry (SOCMI) air oxidation unit processes. (1) APPLICABILITY AND DESIGNATION OF AFFECT

ED FACILITY.(a) The provisions of this section apply to each affected facility designated in par. (b)that produces any of the chemicals listed in sub. (8)as a product, co−product, by−product or intermediate, except as provided in par. (c)

.421 NR 440.675 DEPARTMENT OF NATURAL RESOURCES

The Wisconsin Administrative Code on this web site is current through the last published Wisconsin Register . See also Are the Codes on this Website Official? 

### Register, May 2008, No. 629

(b) The affected facility is any of the following for which construction, modification or reconstruction commenced after October 21, 1983: 1. Each air oxidation reactor not dischar ging its vent stream into a recovery system.2. Each combination of an air oxidation reactor and the recovery system into which its vent stream is dischar ged. 3. Each combination of 2 or more air oxidation reactors and the common recovery system into which their vent streams are discharged. (c) Each affected facility that has a total resource effectiveness (TRE) index value greater than 4.0 is exempt from all provisions of this section except for subs. (3)

, (5) (f)

, (6) (h)and (L)

.

Note: The intent of these standards is to minimize the emissions of VOC through the application of best demonstrated technology (BDT). The numericalemission limits in these standards are expressed in terms of total organic compounds (TOC), measured as TOC minus methane and ethane. This emission limit reflects the performance of BDT. (d) 1. Owners or operators of process vents that are subject to this section may choose to comply with the provisions of 40 CFR part 65 , subpart D, as in effect on December 14, 2000, to satisfy the requirements of subs. (3)to (6) . The provisions of 40 CFR part 65 , subpart D, as in ef fect on December 14, 2000, also satisfy the criteria of par. (c) . Other provisions applying to an

owner or operator who chooses to comply with 40 CFR part 65

, subpart D, as in ef fect on December 14, 2000, are provided in 40 CFR 65.1

. 2. Owners or operators who choose to comply with 40 CFR part 65 , subpart D, as in ef fect on December 14, 2000, shall also comply with ss. NR 440.01

, 440.02

, 440.05

, 440.06

, 440.07 (1) (a)

and (d)

, 440.14 and 440.15 for those process vents. All sections or subsections from ss. NR 440.01 to 440.19 not specified in this subdivision do not apply to owners or operators of process
vents complying with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, except that provisions required to be met prior to implementing 40 CFR part 65 still apply. Owners or operators who choose to comply with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, shall comply with 40 CFR part 65 , subpart A. 3. Owners or operators who choose to comply with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, at initial startup shall comply with subds. 1. and 2. for each vent streamon and after the date on which the initial performance test is completed, but not later than 60 days after achieving the maximum production rate at which the af fected facility will be operated, or 180 days after the initial startup, whichever date comes first. 4. Each owner or operator subject to the provisions of this section that chooses to comply with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, at initial startup shall notify the administrator of the specific provisions of 40 CFR 65.63 (a) (1), (2) or (3) with which the owner or operator has elected to comply. Notification shall be submitted with the notification of initial startup required by 40 CFR 65.5 (b). (2) D EFINITIONS.As used in this section, all terms not defined here shall have the meanings given them in s. NR 440.02 and the following terms shall have the specific meanings given them.(a) “Air oxidation reactor” means any device or process vessel in which one or more organic reactants are combined with airor a combination of air and oxygen, to produce one or more organic compounds. Ammoxidation and oxychlorination reactions are included in this definition.(b) “Air oxidation reactor recovery train” means an individual recovery system receiving the vent stream from at least one air oxidation reactor, along with all air oxidation reactors feeding
vent streams into this system.(c) “Air oxidation unit process” means a unit process, including ammoxidation and oxychlorination unit process, that uses air or a combination of air and oxygen, as an oxygen source in combination with one or more organic reactants to produce one or more organic compounds. (d) “Boilers” means any enclosed combustion device that extracts useful energy in the form of steam.(e) “By compound” means by individual stream components, not carbon equivalents. (f) “Continuousrecorder” means a data recording device recording an instantaneous data value at least once every 15 minutes.(g) “Flame zone” means the portion of the combustion chamber in a boiler occupied by the flame envelope. (h) “Flow indicator” means a device which indicates whether gas flow is present in a vent stream.(i) “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. (j) “Incinerator” means any enclosed combustion device that is used for destroying organic compounds and does not extract energy in the form of steam or process heat.(k) “Process heater” 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.(L) “Process unit” means equipment assembled and connected by pipes or ducts to produce, as intermediate or final products, one or more of the chemicals in sub. (8) . A process unit can operate independently if supplied with suf ficient fuel or raw materials and sufficient product storage facilities. (m) “Product” means any compound or chemical listed in sub. (8)that is produced for sale as a final product as that chemical or is produced for use in a process that needs that chemical for the production of other chemicals in another facility. By− products, co−products and intermediates are considered to be products.(n) “Recovery device” means an individual unit of equipment, such as an ab sorber, condenser and carbon adsorber, capable of and used to recover chemicals for use, reuse or sale. (o) “Recovery system” means an individual recovery device or series of such devices applied to the same process stream.(p) “Total organic compounds” or “TOC” means those compounds measured according to the procedures in sub. (5) (b) 4. For the purposes of measuring molar composition as required in sub. (5) (e) 3. a. , hourly emissions rate as required in sub. (5) (e) 6. and (f) , and TOC concentration as required in sub. (6) (b) 4. and (g) 4. , those compounds which the department has determined do not contribute appreciably to the formation of ozone are to be excluded. The compounds to be excluded are identified in s. NR 400.02 (162)

. (q) “Total resource effectiveness (TRE) index value” means a measure of the supplemental total resource requirement per unit reduction of TOC associated with an individual air oxidation 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 sub. (5) (e)

. (r) “Vent stream” means any gas stream, containing nitrogen which was introduced as air to the air oxidation reactor, releasedto the atmosphere directly from any air oxidation reactor recovery train or indirectly, after diversion through other process equipment. The vent stream excludes equipment leaks and relief valve discharges including, but not limited to, pumps,compressors and valves. (3) S TANDARDS.Each owner or operator of any affected facility shall comply with par. (a)

, (b)or (c) for each vent streamon and after the date on which the initial performance test required by s. NR 440.08 and sub. (5)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 the422 NR 440.675 WISCONSIN ADMINISTRATIVE CODE

The Wisconsin Administrative Code on this web site is current through the last published Wisconsin Register . See also Are the Codes on this Website Official? 

### Register, May 2008, No. 629 initial startup, whichever date comes first. Each owner or operator shall either: (a) Reduce emissions of TOC (minus methane and ethane) by 98 weight− percent or to a TOC (minus methane and ethane) concentration of 20 ppmv on a dry basis corrected to 3% oxygen, whichever is less stringent. If a boiler or process heater is used to comply with this paragraph, then the 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 s. NR 440.18 ; or (c) Maintain a TRE index value greater than 1.0 without use of VOC emission control devices. (4) 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 sub. (3) (a)shall install, calibrate, maintain and operate according to manufacturer’s specifications the following equipment:1. A temperature monitoring device equipped with a continuous recorder and having an accuracy of 1% of the temperature being monitored expressed in degrees Celsius or 0.5 ° C, whichever is greater. a. Where an incinerator other than a catalytic incinerator is used, a temperature monitoring device shall be installed in the firebox.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. A flow indicator that provides a record of vent stream flow to the incinerator at least once every hour for each af fected 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 sub. (3) (b)shall install, calibrate, maintain and op erate according to manufacturer’s specifications the following equipment: 1. A heat sensing device, such as an ultra−violet sensor orthermocouple, 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 af fected facility. The flow indicator 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 sub. (3) (a)shall install, calibrate, maintain and operate according to the manufacturer’s specifications the following equipment: 1. A flow indicator that provides a record of vent stream flow to the boiler or process heater at least once every hour for each af fected facility. The flow indicator shall be installed in the vent stream from each air oxidation reactor within an affected facility at a point closest to the inlet of each boiler or processheater 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% 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. (d) The owner or operator of an affected facility that uses a boiler or process heater to comply with sub. (3) (a)shall monitor and record the periods of operation of the boiler or process heater if the design input capacity of the boiler is 44 MW (150 million Btu/hr) or greater. The records shall be readily available for inspection. (e) The owner or operator of an affected facility that seeks to demonstrate compliance with the TRE index value limit specified under sub. (3) (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 department:1. Where an absorber is the final recovery device in a recovery system:a. A scrubbing liquid temperature monitoring device having an accuracy of  1% 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 witha continuous recorder;b. An organic monitoring device used to indicate the concentration level of or ganic compounds exiting the recovery device based on a detection principle such as infra−red, photoionization or thermal conductivity, each equipped with a continuous recorder.2. Where a condenser is the final recovery device in a recovery system: a. A condenser exit or product side temperature monitoring device equipped with a continuous recorder and having an accuracy of  1% of the temperature being monitoring expressed in degrees Celsius or  0.5 ° C, whichever is greater;b. An organic monitoring device used to indicate the concentration level of or ganic 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 in a recovery system: a. An integrating steam flow monitoring device having an accuracy of  10% and a carbon bed temperature monitoring device having an accuracy of  1% of the temperature being monitored expressed in degrees Celsius or  0.5 ° C, whichever is greater, both equipped with a continuous recorder;b. An organic monitoring device used to indicate the concentration level of or ganic compounds exiting the recovery device based on a detection principle such as infra−red, photoionization or thermal conductivity, each equipped with a continuous recorder. (f) An owner or operator of an affected facility seeking to demonstrate com pliance with the standards specified under sub. (3)with control devices other than an incinerator, boiler, process heater or flare; or recovery devices other than an absorber, condenser or carbon adsorber 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 specify appropriate monitoring procedures or requirements. (5) T EST METHODS AND PROCEDURES.(a) For the purpose of demonstrating compliance with sub. (3) , all af fected facilities shall be run at full operating conditions and flow rates during any performance test. (b) The following methods in Appendix A of 40 CFR part 60 , incorporated by reference in s. NR 440.17 , except as provided under s. NR 440.08 (2) (b) , shall be used as reference methods to determine compliance with the emission limit or percent reduction efficiency specific under sub. (3) (a) :1. Method 1 or 1A, 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 and423 NR 440.675 DEPARTMENT OF NATURAL RESOURCES

The Wisconsin Administrative Code on this web site is current through the last published Wisconsin Register . See also Are the Codes on this Website Official? 

### Register, May 2008, No. 629 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 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 (%O 2d) 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% O 2(C c) shall be computed using the following equations:

C c C TOC 17.9 20.9

 %0 2d where: C cis the concentration of TOC corrected to 3% O 2 , dry basis, ppm by volume C TOCis the concentration of TOC (minus methane and ethane), dry basis, ppm by volume %O 2d is the concentration of O 2 , dry basis, percent by volume 4. Method 18 to determine concentration of TOC in the control device outlet and the concentration of TOC in the inlet when the reduction ef ficiency of the control device is to be determined. a. The sampling time for each run shall be 1 hour in which either an integrated sample or 4 grab samples shall be taken. If grab sampling is used then the samples shall be taken at 15−minute intervals. b. The emission reduction (R) of TO C (minus methane and ethane) shall be determined using the following equation:

R E i–E o E i  100
where: R is the emission reduction, percent by weight E iis the mass rate of TOC entering the control device, kg/hr (lb/hr) E ois the mass rate of TOC discharged to the atmosphere, kg/hr (lb/hr) c. The mass rates of TOC (Ei, Eo) shall be computed using the following equations:

E i K 2 

#   n

j 1 C ij M ij 

#  Q i

E o K 2 

#   n

j 1 C oj M oj 

#  Q o

where: C ij and C oj are the concentration of sample component “j” of the gas stream at the inlet and outlet of the control device, respectively, dry bas is, ppm by volume Mij and Moj are the molecular weight of sample component “j” of the gas stream at the inlet and outlet of the control device, respectively, g/g−mole (lb/lb−mole) Q iand Qoare the flow rate of gas stream at the inlet and outlet of the control device, respectively, dscm/min (dscf/min) K2is a constant, 2.494 x 10 −6(1/ppm)(g−mole/ scm)(kg/g)(min/hr) for metric units, where standard temperature for (g−mole/scm) is 20 C, and 1.557 x 10 −7(1/ppm)(lb−mole/ scf)(min/hr) for English units, where standard temperature for (lb−mole/scf) is 68 F d. The TOC concentration (C TOC) is the sum of the individual components and shall be computed for each run using the following equation: where: C TOC 

#  n

j 1 C j

C TOCis the concentration of TOC (minus methane and ethane), dry basis, ppm by volume C

j is the concentration of sample components in the sample n is the number of components in the sample (c) 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 sub. (3) (a) , the requirement for an initial performance test is waived, in accordance with s. NR 440.08 (2)

. However, the department reserves the option to requiretesting at such other times as may be required. (d) When a flare is used to seek to comply with sub. (3) (b)

, the flare shall comply with the requirements of s. NR 440.18

. (e) The following test methods in Appendix A of 40 CFR part 60 , incorporated by reference in s. NR 440.17 , except as provided under s. NR 440.08 (2) , shall be used for determining the net heating value of the gas combusted to determine compliance under sub. (3) (b)and for determining the process vent stream TRE index value to determine compliance under sub. (3) (c)

.1. Method 1 or 1A, as appropriate, for selection of the sampling site. The sampling site for the vent stream flow rate and molar composition determination prescribed in subds. 3. and 4. shall be, except for the situations outlined in subd. 2. , prior to the inlet of any control device, prior to any post−reactor dilution of the stream with air and prior to any post−reactor introduction of halogenated compounds into the vent stream. No transverse site selection method is needed for vents smaller than 10 centimeters (4 inches) in diameter. 2. If any gas stream other than the air oxidation vent stream from the af fected facility is normally conducted through the final
recovery device: a. The sampling site for vent stream flow rate and molar composition shall be prior to the final recovery device and prior to the point at which the nonair oxidation stream is introduced. b. The ef ficiency 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 nonair oxidation 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 nonair oxidation stream to determine the concentration of TOC in the air oxidation stream from the final recovery device. This concentration of TOC is then used to perform the calculations outlined in subds. 5. and 6. 3. The molar composition of the process vent stream shall be determined as follows:a. Method 18 to measure the concentration of TOC including those containing halogens. b. ASTM D1946−90 (reapproved 1994), incorporated by reference in s. NR 440.17 (2) (a)24., to measure the concentration of carbon monoxide and hydrogen. c. Method 4 to measure the content of water vapor.4. The volumetric flow rate shall be determined using Method 2, 2A, 2C or 2D, as appropriate.5. The net heating value of the vent stream shall be calculated using the following equation:

H T K 1 

#   n

j 1 Cj Hj 

# 

where: H Tis the net heating value of the sample, MJ/scm (Btu/scf),where the net enthalpy per mole of vent stream is based on combustion at 25 ° C and 760 mm Hg (77 F and 30 in Hg), but the424 NR 440.675 WISCONSIN ADMINISTRATIVE CODE

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### Register, May 2008, No. 629 standard temperature for determining the volume corresponding to one mole is 20 ° C (68 ° F) K 1 is a constant, 1.740 x 10 −7(1/ppm)(g−mole/scm)(MJ/ kcal) for metric units where standard temperature for (g−mole/ scm) is 20 C, and 1.03 x 10−11 (1/ppm)(lb−mole/scf)(Btu/kcal) for English units where standard temperature for (lb−mole/scf) is 68 F C

j is the concentration on a wet basis of compound j in ppm, as measured for or ganics by Method 18 and measured for hydrogen and carbon monoxide by ASTM D1946−90 (reapproved 1994), incorporated by reference in s. NR 440.17 (2) (a)24., as indicated in subd 3. H

j is the net heat of combustion of compound j, kcal/g−mole (kcal/lb−mole), based on combustion at 25 C and 760 mm Hg (77 F and 30 in Hg). The heats of combustion of vent stream components would be required to be determined using ASTM D2382−88 or D4809−95, incorporated by reference as specified in s. NR 440.17 (2) (a)30. and 61., if published values are not available or cannot be calculated 6. The emission rate of TOC in the process vent stream shall be calculated using the following equation:

E TOC K 2 

#   n

j 1 Cj Mj 

#  Q s

where: E TOCis the emission rate of TOC in the sample, kg/hr (lb/hr)

K2is the constant, 2.494  10 −6(1/ppm) (g−mole/scm) (kg/g) (min/hr) for metric units, where standard temperature for (g−mole/scm) is 20 C, and 1.557 x 10 −7(1/ppm)(lb−mole/ scf)(min/hr) for English units, where standard temperature for (lb−mole/scf) is 68 F C

j is the concentration on a wet basis of compound j in ppm as measured by Method 18 as indicated in subd. 3. M

j is the molecular weight of sample j, g/g−mole (lb/lb− mole) Q sis the vent stream flow rate (scm/min) (scf/hr) at a standard temperature of 20 ° C (68 F) 7. 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. (f) For purposes of complying with sub. (3) (c) , the owner or operator of a facility affected by this section shall calculate theTRE index value of the vent stream using the equation for incineration in subd. 1. 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 subd. 1. and the flare equation in subd. 2. and selecting the lower of the 2 values. 1. The TRE index value of the vent stream controlled by an incinerator shall be calculated using the following equation:

TRE 1 E TOC a b  Q s  0.88 c  Q s  d Q s   H T  e  Q s  0.88  H T  0.88 f  Y s  0.5
a. Where for a vent stream flow rate that is greater than or equal to 14.2 scm/min (501 scf/min) at a standard temperature of 20 C (68 F): TRE is the TRE index value Q sis the vent stream flow rate scm/min (scf/min), at a standard temperature of 20 ° C (68 F) H Tis the vent stream net heating value , MJ/scm (Btu/scf), where the net enthalpy per mole of vent stream is based on combustion at 25 C and 760 mm Hg (68 F and 30 in Hg), but the standard temperature for determining the volume corresponding to one mole is 20 C (68 F), as in the definition of Q s Y s= Qsfor all vent stream categories listed in T able 1 except for Category E vent streams where Ys= (Q s ) (HT)/3.6 for metric units and Y s= (Q s )(HT)/97 for English units E TOCis the hourly emissions of TOC, kg/hr (lb/hr) a, b, c, d, e and f are coef ficients The set of coefficients which apply to a vent stream shall be obtained from Table 1. Table 1. Air Oxidation NSPS TRE Coefficients For Vent Streams Controlled By an Incinerator
Design Category A1. For Halogenated Process Vent Streams,
If 0 Net Heating Value (MJ/scm) 3.5 Or If 0 Net Heating Value (Btu/scf) 94: Q s= Vent Stream Flow Rate scm/min (scf/min) a b c d e f
1) 14.2 Q s 1 8.8 (501 Qs 664) 19.18370 (42.29238) 0.27580 (0.017220) 0.75762 (0.072549) −0.13064 (−0.00030361) 0 (0) 0.01025 (0.003803)

2) 18.8 < Q s 699 (664 < Qs 24,700) 20.00563 (44.10441) 0.27580 (0.017220) 0.30387 (0.029098) −0.13064 (−0.00030361) 0 (0) 0.01025 (0.003803)

3) 699 < Q s 1400 (24,700 < Qs 49,000) 39.87022 (87.89789) 0.29973 (0.018714) 0.30387 (0.029098) −0.13064 (−0.00030361) 0 (0) 0.01449 (0.005376)

4) 1400 < Q s 2100 (49,000 < Qs 74000) 59.73481 (131.6914) 0.31467 (0.019647) 0.30387 (0.029098) −0.13064 (−0.00030361) 0 (0) 0.01775 (0.006585)

5) 2100 < Q s 2800 (74,000 < Qs 99,000) 79.59941 (175.4849) 0.32572 (0.020337) 0.30387 (0.029098) −0.13064 (−0.00030361) 0 (0) 0.02049 (0.007602)

6) 2800 < Q s 3500 (99,000 < Qs 120,000) 99.46400 (219.2783) 0.33456 (0.020888) 0.30387 (0.029098) −0.13064 (−0.00030361) 0 (0) 0.02291 (0.008500)
Design Category A2. For Halogenated Process Vent Streams, If Net Heating Value > 3.5 MJ/scm Or If Net Heating Value > 94 (Btu/scf): Q s= Vent Stream Flow Rate scm/min (scf/min) a b c d e f 7) 14.2 Q s 18.8 (501 Qs 664) 18.84466 (41.54494) 0.26742 (0.016696) −0.20044 (−0.019194) 0 (0) 0 (0) 0.01025 (0.003803) 8) 18.8 < Q s 699 (664 < Qs 24,700) 19.66658 (43.35694) 0.26742 (0.016696) −0.25332 (−0.024258) 0 (0) 0 (0) 0.01025 (0.003803)425 NR 440.675 DEPARTMENT OF NATURAL RESOURCES

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### Register, May 2008, No. 629 Table 1. Air Oxidation NSPS TRE Coefficients For Vent Streams Controlled By an Incinerator (continued)
Design Category A2. For Halogenated Process Vent Streams, If Net Heating Value > 3.5 MJ/scm Or If Net Heating Value > 94 (Btu/scf): Q s= Vent Stream Flow Rate scm/min (scf/min) a b c d e f
9) 699 < Q s 1400 (24,700 < Qs 49,000) 39.19213 (86.40297) 0.29062 (0.018145) −0.25332 (−0.024258) 0 (0) 0 (0) 0.01449 (0.005376)
10) 1400 < Q s 2100 (49,000 < Qs 74000) 58.71768 (129.4490) 0.30511 (0.019050) −0.25332 (−0.024258) 0 (0) 0 (0) 0.01775 (0.006585)
11) 2100 < Q s 2800 (74,000 < Qs 99,000) 78.24323 (172.4950) 0.31582 (0.019718) −0.25332 (−0.024258) 0 (0) 0 (0) 0.02049 (0.007602)
12) 2800 < Q s 3500 (99,000 < Qs 120,000) 97.76879 (215.5411) 0.32439 (0.020253) −0.25332 (−0.024258) 0 (0) 0 (0) 0.02291 (0.008500)

Design Category B. For Nonhalogenated Process Vent Streams,

If 0  Net Heating Value (MJ/scm)  0.48 Or If 0 Net Heating Value (Btu/scf) 13: Q s= Vent Stream Flow Rate scm/min (scf/min) a b c d e f 13) 14.2 Q s 1340 (501 Qs 47,300) 8.54245 (18.83268) 0.10555 (0.0065901) 0.09030 (0.008647) −0.17109 (−0.00039762) 0 (0) 0.01025 (0.003803)
14) 1340 < Q s 2690 (47,300 < Qs 95,000) 16.94386 (37.35443) 0.11470 (0.0071614) 0.09030 (0.008647) −0.17109 (−0.00039762) 0 (0) 0.01449 (0.005376)
15) 2690 < Q s 4040 (95,000 < Qs 143,000) 25.34528 (55.87620) 0.12042 (0.0075185) 0.09030 (0.008647) −0.17109 (−0.00039762) 0 (0) 0.01775 (0.00658)

Design Category C. For Nonhalogenated Process Vent Streams,

If 0.48 Net Heating Value (MJ/scm)  1.9 Or If 13 < Net Heating Value (Btu/scf) 51: Q s= Vent Stream Flow Rate scm/min (scf/min) a b c d e f 16) 14.2 Q s 1340 (501 Qs 47,300) 9.25233 (20.39769) 0.06105 (0.003812) 0.31937 (0.030582) −0.16181 (−0.00037605) 0 (0) 0.01025 (0.003803)
17) 1340 < Q s 2690 (47,300 < Qs 95,000) 18.36363 (40.48446) 0.06635 (0.004143) 0.31937 (0.030582) −0.16181 (−0.00037605) 0 (0) 0.01449 (0.005376)
18) 2690 < Q s 4040 (95,000 < Qs 143,000) 27.47492 (60.57121) 0.06965 (0.004349) 0.31937 (0.030582) −0.16181 (−0.00037605) 0 (0) 0.01775 (0.006585)

Design Category D. For Nonhalogenated Process Vent Streams,

If 1.9 Net Heating Value (MJ/scm)  3.6 Or If 51 < Net Heating Value (Btu/scf) 97: Q s= Vent Stream Flow Rate scm/min (scf/min) a b c d e f 19) 14.2 Q s 1180 (501 Qs 41,700) 6.67868 (14.72382) 0.06943 (0.004335) 0.02582 (0.002472) 0 (0) 0 (0) 0.01025 (0.003803)
20) 1180 < Q s 2370 (41,000 < Qs 83,700) 13.21633 (29.13672) 0.07546 (0.004711) 0.02582 (0.002472) 0 (0) 0 (0) 0.01449 (0.005376)
21) 2370 < Q s 3550 (83,700 < Qs 125,000) 19.75398 (43.54962) 0.07922 (0.004946) 0.02582 (0.002472) 0 (0) 0 (0) 0.01775 (0.00658)

Design Category E. For Nonhalogenated Process Vent Streams, If Net Heating Value > 3.6 MJ/scm Or If Net Heating Value > 97 Btu/scf):

Ys= Dilution Flow Rate scm/min = (Q s)(H T)/3.6 (scf/min) = (Qs)(HT)/97 a b c d e f 22) 14.2 Ys 1180 (501 Y s 41,700) 6.67868 (14.72382) 0 (0) 0 (0) −0.00707 (−0.0000164) 0.02220 (0.0001174) 0.01025 (0.003803)
23) 1180 < Ys 2370 (41,700 < Y s 83,700) 13.21633 (29.13672) 0 (0) 0 (0) −0.00707 (−0.0000164) 0.02412 (0.0001276) 0.01449 (0.005376)
24) 2370 < Ys 3550 (83,700 < Y s 125,000) 19.75398 (43.54962) 0 (0) 0 (0) −0.00707 (−0.0000164) 0.02533 (0.0001340) 0.01775 (0.006585)

b. Where for a vent stream flow rate that is less than 14.2 scm/min (501 scf/min) at a standard temperature of 20 C (68 F): TRE is the TRE index value Q sis 14.2 scm/min (501 scf/min)
H Tis (FLOW) (HVAL) / Q s where the following inputs are used: FLOW is the vent stream flow rate (scm/min) (scf/min), at a standard temperature of 20 ° C (68 ° F) HVAL is the vent stream net heating value MJ/scm (Btu/scf), where the net enthalpy per mole of vent stream is based on combustion at 25 ° C and 760 mm Hg (77 F and 30 in Hg), but the standard temperature for determining the volume corresponding to 1 mole is 20 ° C (68 F) as in the definition of Q s426 NR 440.675 WISCONSIN ADMINISTRATIVE CODE

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### Register, May 2008, No. 629 Y s= Qsfor all vent stream categories listed in Table 1 except for Category E vent streams, where Y s= Q s H T/3.6 for metric units and Y s= Q s H T/97 for English units.

E TOCis the hourly emissions of TOC reported in kg/hr (lb/hr) a,b,c,d,e and f are coef ficients
The set of coef ficients that apply to a vent stream shall 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 1 E TOC [a(Q s ) b(Q s ) 0.8 c(Q s )(H T) d(E TOC ) e] where: TRE is the TRE index value
E TOCis the hourly emissions of TOC, kg/hr (lb/hr) Q sis the vent stream flow rate, scm/min (scf/min) at a standard temperature of 20 ° C (68 ° F) H Tis the vent stream net heating value, MJ/scm (Btu/scf), where the net enthalpy per mole of vent stream is based on combustion at 25 ° C and 760 mm Hg (77 F and 30 in Hg), but the standard temperature for determining the volume corresponding to 1 mole is 20 ° C (68 F) as in the definition of Q s a,b,c,d and e are coef ficients The set of coef ficients that apply to a vent stream shall be obtained from Table 2.

Table 2. Air Oxidation Processes NSPS TRE Coefficients For Vent Streams Controlled By a Flare

a b c d e

a. HT< 11.2 MJ/scm (HT< 301 Btu/scf) 2.25 (0.140) 0.288 (0.0367) −0.193 (−0.000448) −0.0051 (−0.0051) 2.08 (4.59)

b. HT  11.2 MJ/scm (HT  301 Btu/scf) 0.309 (0.0193) 0.0619 (0.00788) −0.0043 (−0.000010) −0.0034 (−0.0034) 2.08 (4.59)
(g) Each owner or operator of an affected facility seeking to comply with sub. (1) (c)or (3) (c)shall recalculate the TRE index value for that af fected facility whenever process changes aremade. Some examples of process changes are changes in production capacity, feedstock type or catalyst type or wheneverthere is replacement, removal or addition of recovery equipment. The TRE index value shall be recalculated based on test data or on b est 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 departmentwithin 1 week of the recalculation and shall conduct a performance test according to the methods and procedures required by sub. (5)to determine compliance with sub. (3) (a) . Performance tests shall be conducted as soon as possible after the process change but no later than 180 days from the time of the process change. 2. Where the initial TRE index value is greater than 4.0 and the recalculated TRE index value is less than or equal to 4.0, butgreater than 1.0, the owner or operator shall conduct a performance test in accordance with s. NR 440.08and this subsection, and shall comply with subs. (4)and (6)and this subsection. Performance tests shall be conducted as soon as possible after the process change but no later than 180 days from the time of the process change. (6) REPORTING AND RECORDKEEPING REQUIREMENTS. (a) Each owner or operator subject to sub. (3)shall notify the department of the specific provisions of sub. (3)with which the owneror operator has elected to comply. Notification shall be submitted with the notification of initial startup required by s. NR 440.07 (1) (c) . If an owner or operator elects at a later date to use an alternative provision of sub. (3)with which he or she will comply, then the department 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 sub. (5)within 180 days. (b) Each owner or operator subject to the provisions of this section shall keep up−to−date, readily accessible records 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 s. NR 440.08 . 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 sub. (3) (a) , a report containing performance test data need not be submitted, but a report containing the information of subd. 2. a. is required. The same data specified in this su bsection shall be submitted in the reports of all subsequently required performance 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 this section seeks to demonstrate compliance with sub. (3) (a)through use of either a thermal or catalytic incinerator: a. 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 minutesand averaged over the same time period of the performance testing, and b. The percent reduction of TOC determined as specified in sub. (5) (b)achieved by the incinerator or the concentration of TOC (ppmv, by compound) determined as specified in sub. (5) (b)at the outlet of the control device on a dry basis corrected to 3% oxygen. 2. Where an owner or operator subject to the provisions of this section seeks to demonstrate compliance with sub. (3) (a) through use of a boiler or process heater: a. A description of the location at which the vent stream is introduced into the boiler or process heater, andb. 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 section seeks to comply with sub. (3) (b)through the use ofa smokeless flare, flare design, that is, steam−assisted, air−assisted or nonassisted, all visible emission readings, heat contentdeterminations, 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 seeks to demonstrate compliance with sub. (3) (c)

.a. Where an absorber is the final recovery device in a recovery system, the exit specific gravity, or alternative parameter which is a measure of the degree of absorbing liquid saturation, if approved by thedepartment, and average exit temperature of the absorbing 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; or427 NR 440.675 DEPARTMENT OF NATURAL RESOURCES

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### Register, May 2008, No. 629b. Where a condenser is the final recovery device in a recovery system, the average exit, that is, product side, temperature, measured at least every 15 minutes and average over the same time period of the performance testing while the vent stream is normally routed and constituted. c. Where a carbon adsorber is the final recovery device in arecovery system, the total steam mass flow measured at least every 15 minutes and averaged over the same time period of the performance test, that is, full carbon bed cycle, temperature of the carbon bed after regeneration, and within 15 minutes of completion of any cooling cycle, and duration of the carbon bed steaming cycle, all measured while the vent stream is normally routed and constituted; or d. As an alternative to subd. 4. a.

, b. or c. , the concentration level or reading indicated by the or ganic 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.e. 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 section shall keep up−to−date, readily accessible continuous records of the equipment operating parameters specified to be monitored under sub. (4) (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 department may at any time require a report of these data. Where a combustion device is used by an
owner or opera tor seeking to demonstrate compliance with sub. (3) (a)or (c), periods of operation during which the parameter boundaries esta blished 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 temperature of the ventstream during the most recent performance test at which compliance with sub. (3) (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) belowthe average temperature of the vent stream during the most recent p erformance test at which compliance with sub. (3) (a)was determined. The owner or operator also shall record all 3−hourperiods of operation during which the average temperature difference across the catalyst bed is less than 80% of the average temperature difference of the device during the most recent performance test at which compliance with sub. (3) (a)was determined. 3. All 3−hour periods of operation during which the average combustion temperature was more than 28 ° C (50 ° F) below theaverage combustion temperature during the most recent performance test at which compliance with sub. (3) (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 sub. (3) (a)

. (d) Each owner or operator subject to the provisions of this section shall keep up−to−date, readily accessible continuous records of the flow indication specified under sub. (4) (a) 2.

, (b) 2. and (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. (e) Each owner or operator subject to the provisions of this section who uses a boiler or process heater with a design heat input capacity of 44 MW (150 million Btu/hour) or greater to comply with sub. (3) (a)shall keep an up−to−date, readily accessible record of all periods of operation of the boiler or process heater.

Note: Examples of such records could include records of steam use, fuel use or monitoring data collected pursuantto other state or federal regulatory requirements. (f) Each owner or operator subject to the provisions of this section shall keep up−to−date, readily accessible continuous records of the flare pilot flame monitoring specified in sub. (4) (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 section shall keep up−to−date, readily accessible continuous records of the equipment operating parameters specified to be monitored under sub. (4) (e)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 department may at any time require a report of these data. Where the owner or operator seeks to demonstrate compliance with sub. (3) (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 monitoring device is not used: a. 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 b. 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 liquid saturation, is approved by the department, in which case the department will define appropriate parameter boundaries and periods of operation during which they are exceeded. 2. When a condenser is the final recovery device in a recovery system and where an organic monitoring device is not used, all 3−hour periods of operation during which theaverage exit or product side condenser operating temperature was more than 6 ° C (11 ° 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 recovery system and where an organic monitoring device is not used: a. All carbon bed regeneration cycles during which the total mass steam flow was more than 10% below the total mass steam flow during the most recent performance test; orb. All carbon bed regeneration cycles during which the temperature of the carbon bed after regeneration, and after completion of any cooling cycle, was more than 10% 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 an organic monitoring device approved by the department is used, all3−hour periods of operation during which the average concentration level or reading of or ganic compounds in the exhaust gases is more than 20% 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 subject to the provisions of this section and seeking to demonstrate compliance with sub. (3) (c) shall keep up−to−date, readily accessible records of: 1 . Any changes in production capacity, feedstock type or of any replacement, removal or addition of recovery equipment or air oxidation reactors;428 NR 440.675 WISCONSIN ADMINISTRATIVE CODE

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### Register, May 2008, No. 6292. Any recalculation of the TRE index value performed pursuant to sub. (5) (f) ; 3. The results of any performance test performed pursuant to the methods and procedures required by sub. (5) (d)

. (i) Each owner and operator subject to the provisions of this section is exempt from the quarterly reporting requirements contained in s. NR 440.07 (3)

.(j) Each owner or operator that seeks to comply with the requirements of this section by complying with the requirements of sub. (3)shall submit to the department semiannual reports of the following information. The initial report shall be submitted within 6 months after the initial startup date. 1. Exceedances of monitored parameters recorded under
pars. (c) and (g)

. 2. All periods recorded under par. (d)when the vent stream is diverted from the control device or has no flow rate. 3. All periods recorded under par. (e)when the boiler or process heater was not operating. 4. All periods recorded under par. (f)in which the pilot flame of the flare was absent. 5. Any recalculation of the TRE index value, as recorded under par. (h)

.

Note: The requirements of par. (j) remain in 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 par. (j), provided that they comply with the requirements established by the state. (L) The department will specify appropriate reporting and recordkeeping re quirements where the owner or operator of an affected facility seeks to demonstrate compliance with the standards specified under sub. (3)other than as provided under sub. (4) (a)to (d)

. (7) RECONSTRUCTION.(a) For purposes of this section “fixed capital cost of the new components”, as used in s. NR 440.15

, includes the fixed capital cost of all depreciable componentswhich are or will be replaced pursuant to all continuous programs of components which are commenced within any 2−yearperiod following October 21, 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. (8) C HEMICALS AFFECTED BY THIS SECTION.

Chemical Name CAS No.* (a) Acetaldehyde . . . . . . . . . . . . . . . . . . . . . . 75−07−0 (b) Acetic acid . . . . . . . . . . . . . . . . . . . . . . . . 64−19−7 (c) Acetone . . . . . . . . . . . . . . . . . . . . . . . . . . 67−64−1 (d) Acetonitrile . . . . . . . . . . . . . . . . . . . . . . . . 75−05−8 (e) Acetophenone . . . . . . . . . . . . . . . . . . . . . . 98−86−2 (f) Acrolein . . . . . . . . . . . . . . . . . . . . . . . . . . 107−02−8 (g) Acrylic acid . . . . . . . . . . . . . . . . . . . . . . . 79−10−7 (h) Acrylonitrile . . . . . . . . . . . . . . . . . . . . . . . 107−13−1 (i) Anthraquinone . . . . . . . . . . . . . . . . . . . . . 84−65−1 (j) Benzaldehyde . . . . . . . . . . . . . . . . . . . . . . 100−52−7 (k) Benzoic acid, tech . . . . . . . . . . . . . . . . . . . 65−85−0 (L) 1,3−Butadiene . . . . . . . . . . . . . . . . . . . . . . 106−99−0 (m) p−t−Butyl benzoic acid . . . . . . . . . . . . . . . 98−73−7 (n) N−Butyric acid . . . . . . . . . . . . . . . . . . . . . 107−92−6 (o) Crotonic acid . . . . . . . . . . . . . . . . . . . . . . 3724−65−0 (p) Cumene hydroperoxide . . . . . . . . . . . . . . 80−15−9 (q) Cyclohexanol . . . . . . . . . . . . . . . . . . . . . . 108−93−0 (qm) Cyclohexanone . . . . . . . . . . . . . . . . . . . . . 108−94−1 (r) Dimethyl terephthalate . . . . . . . . . . . . . . . 120−61−6 Chemical Name CAS No.* (rm) Ethylene dichloride . . . . . . . . . . . . . . . . . . 107−06−2 (s) Ethylene oxide . . . . . . . . . . . . . . . . . . . . . 75−21−8 (sm) Formaldehyde . . . . . . . . . . . . . . . . . . . . . . 50−00−0 (t) Formic acid . . . . . . . . . . . . . . . . . . . . . . . . 64−18−6 (tm) Glyoxal . . . . . . . . . . . . . . . . . . . . . . . . . . . 107−22−2 (u) Hydrogen cyanide . . . . . . . . . . . . . . . . . . 74−90−8 (um) Isobutyric acid . . . . . . . . . . . . . . . . . . . . . 79−31−2−5 (v) Isophthalic acid . . . . . . . . . . . . . . . . . . . . . 121−91 (vm) Maleic anhydride . . . . . . . . . . . . . . . . . . . 108−31−6 (w) Methyl ethyl ketone . . . . . . . . . . . . . . . . . 78−93−3 (wm) −Methyl styrene . . . . . . . . . . . . . . . . . . . 98−83−9 (x) Phenol . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−95−2 (xm) Phthalic anhydride . . . . . . . . . . . . . . . . . . 85−44−9 (y) Propionic acid . . . . . . . . . . . . . . . . . . . . . . 79−09−4 (ym) Propylene oxide . . . . . . . . . . . . . . . . . . . . 75−56−9 (z) Styrene . . . . . . . . . . . . . . . . . . . . . . . . . . . 100−42−5 (zm) Terephthalic acid . . . . . . . . . . . . . . . . . . . 100−21−0

*CAS numbers refer to the Chemical Abstracts Service Registry numbers assigned to specific isomers or mixtures of chemicals. 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 listed, whether CAS numbers have been assigned or not.

History: Cr. Register, July , 1993, No. 451 , eff. 8−1−93 ; am. (4) (a) 1. (intro.), (d) 1. a., 3. a., (5) (e) 1. a., Register, December, 1995, No. 480 , eff. 1−1−96 ;
renum. (2) (a) (intro.) and 1. to 18. to be (2) (intro.) and (a) to (r), am. (2) (p), Register, November, 1999, No. 527 , eff. eff. 12−1−99; CR 06−109 : cr. (1) (d),

renum. (4) (c) 3. to be (4) (d) and am., renum. (4) (d) and (e) to be (4) (e) and (f), renum. (5) (b) 5., (c), (d), (e) and (f) to be (5) (c), (d), (e), (f) and (g) and am. (5) (e) 1., 3. b., 5. and 6. and (f) 1. a. and b., am. (5) (b) 4. b. and c., (6) (e) and (g) (intro.) and (8) Register May 2008 No. 629 , eff. 6−1−08; corrections in (1) (d) 2. and (2) (p) made under s. 13.92 (4) (b) 7. , Stats., Register May 2008 No. 629

. NR 440.68 Petroleum dry cleaners. (1) APPLICABIL

ITY AND DESIGNATION OF AFFECTED FACILITY.(a) The provisions of this section are applicable to the following affected facilities located at a petroleum dry cleaning plant with a total manufacturer’s rated dryer capacity equal to or greater than 38 kilograms (84 pounds): Petroleum solvent dry cleaning dryers, washers, filters, stills and settling tanks. 1. When the affected facility is installed in an existing plant that is not expanding the manufacturer’s rated capacity of its petroleum solvent dryer(s) the total manufacturer ’s rated dryer capacity is the summation of the manufacturer’s rated capacity for each existing petroleum solvent dryer. 2. When the affected facility is installed in a plant that is expanding the manufacturer’s rated capacity of its petroleum solvent dryers the total manufacturer’s rated dryer capacity is the summation of the manufacturer’s rated dryer capacity for each existing and proposed new petroleum solvent dryer. 3. When the affected facility is installed in a new plant the total manufacturer’s rated dryer capacity is the summation of the manufacturer’s rated dryer capacity for each proposed new petroleum solvent dryer.4. The petroleum solvent dryers considered in the determination of the total manufacturer’s rated dryer capacity are those new and existing dryers in the plant that will bein serviceat any time after the proposed new source or modification commences operation. (b) Any facility under par. (a) that commences construction or modification after December 14, 1982, is subject to the requirements of this section, except that a dryer installed between December 14, 1982 and September 21, 1984, in a plant with an annual solvent consumption level of less than 17,791 liters (4,700 gallons), is exempt from the requirements of this section.435 NR 440.686 DEPARTMENT OF NATURAL RESOURCES

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### Register, May 2008, No. 629 the same end point. Call the ml of iodine used C. Then,

Grains H 2 S per 100 cubic foot of gas 100 (D

 C) (f) Sensitivity enhancement. 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. Usuallythe starch−iodine end point is much less distinct and a blank determination of end point, with H2 S−free gas or air, is required.

Figure 1. Tutwiler burette (lettered items mentioned in text).

History: Cr. Register, September, 1990, No. 417 , eff. 10−1−90; am. (2) (a) 4., (4) (b), (7) (a) 2. and 4., (b) 3., (c), (d) (intro.), (e) and (8) (a), renum. (2) (b) 4. to 6. to be (2) (b) 5. to 7., cr. (2) (b) 4., r. and recr. (5), r. (6), Register, July, 1993, No. 451 , eff. 8−1−93; am. (5) (c) 3., Register, December, 1995, No. 480 , eff. 1−1−96; CR 06−109 : am. (2) (a) 8. and (b) 1. to 3., (4) (b), (5) (b) 1. to 3., (c) 2. and 4. and (7) (b) 1. and (c), r. (2) (b) 4., renum. (2) (b) 5. to 7. to be (2) (b) 4. to 5. and am., r. and recr. (5) (c) 3. and (7) (e) Register May 2008 No. 629 , eff. 6−1−08. NR 440.686 Volatile organic compound (VOC) emissions from synthetic organic chemical manufacturing industry (SOCMI) distillation operations. (1) APPLICABILITY AND DESIGNATION OF AFFECTED FACILITY. (a) The provisions of this section apply to each affected facility designated in par. (b)that is part of a process unit that produces any of the chemicals listed in sub. (8)as a product, co−product, by− product or intermediate, except as provided in par. (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 common recovery system into which its vent stream is di scharged. 3. Each combination of 2 or more distillation units and thecommon recovery system into which their vent streams are discharged. (c) Exemptions from the provisions of par. (a) are as follows: 1. Any distillation unit operating a part of a process unit which produces coal tar or beverage alcohols or which uses, contains and produces no VOC is not an af fected facility. 2. Any distillation unit that is subject to the provisions of s. NR 440.647is not an affected facility. 3. Any distillation unit that is designed and operates as a batch operation is not an af fected facility. 4. Each af fected facility that has a total resource effectiveness (TRE) index value greater than 8.0 is exempt from all provisions of this section except for subs. (3)

, (5) (d)

, (e) and (f)and (6) (h)and (L)

. 5. Each af fected facility in a process unit with a total design capacity for all chemicals produced within that unit of less than one gigagram per year is exempt from all provisions of this section except for the recordkeeping and reporting requirements in sub. (6) (j)

, (L) 6. and (n)

. 6. Each affected facility operated with a vent stream flow
rate less than 0.008 scm/min is exempt from all provisions of this section except for the test method and procedure and the recordkeeping and reporting requirements in subs. (5) (g)and (6) (i)

, (L) 5. and (o)

.

Note: The intent of these standards is to minimize the emissions of VOC through the application of best demonstrated technology (BDT). The numericalemission limits in these standards are expressed in terms of total organic compounds (TOC), measured as TOC less methane and ethane. This emission limit reflects the performance of BDT. (d) 1. Owners or operators of process vents that are subject to this section may choose to comply with the provisions of 40 CFR part 65 , subpart D, as in effect on December 14, 2000, to satisfy the requirements of subs. (3)to (6) . The provisions of 40 CFR part 65 , subpart D, as in ef fect on December 14, 2000, also satisfy the criteria of par. (c) 4. and 6. Other provisions applying to an owner or operator who chooses to comply with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, are provided in 40 CFR 65.1

. 2. Owners or operators who choose to comply with 40 CFR part 65 , subpart D, as in ef fect on December 14, 2000, shall also comply with ss. NR 440.01

, 440.02

, 440.05

, 440.06

, 440.07 (1) (a)

and (d)

, 440.14 and 440.15 for those process vents. All sections or subsections from ss. NR 440.01 to 440.19 not specified in this subdivision do not apply to owners or operators of process
vents complying with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, except that provisions required to be met prior to implementing 40 CFR part 65 still apply. Owners or operators who choose to comply with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, shall comply with 40 CFR part 65 , subpart A. 3. Owners or operators who choose to comply with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, at initial startup shall comply with subds. 1. and 2. for each vent streamon and after the date on which the initial performance test is completed, but not later than 60 days after achieving the maximum production rate at which the af fected facility will be operated, or 180 days after the initial startup, whichever date comes first. 4. Each owner or operator subject to the provisions of this section that chooses to comply with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, at initial startup shall notify the administrator of the specific provisions of 40 CFR 65.63 (a) (1), (2) or (3), as in ef fect on December 14, 2000, with which the

owner or operator has elected to comply. Notification shall be submitted with the notification of initial startup required by 40 CFR 65.5 (b).436 NR 440.686 WISCONSIN ADMINISTRATIVE CODE

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### Register, May 2008, No. 629

(2) D EFINITIONS.As used in this section, all terms not defined here shall have the meaning given them in s. NR 440.02 and the following terms shall have the specific meanings given them: (a) “Batch distillation operation” means a noncontinuous 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 char ging of the liquid feed, no additional liquid is added during the distillation operation.(b) “Boiler” means any enclosed combustion device that extracts useful energy in the form of steam. (c) “By compound” means by individual steam components, not carbon equivalents.(d) “Continuous recorder” means a data recording device recording an instantaneous data value at least once every 15 minutes. (e) “Distillation operation” means an operationseparating one or more feed streams into 2 or more exit streams, each exit stream ha ving component concentrations different from those in the feed streams. The separation is achieved by the redistribution of the components between the liquid and va por− phase as they approach equilibrium within the distillation unit.(f) “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 or other similar device, plus any associated recovery system.(g) “Flame zone” means the portion of the combustion chamber in a boiler occupied by the flame envelope. (h) “Flow indicator” means a device which indicates whether gas flow is present in a vent stream.(i) “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. (j) “Incinerator” means any enclosed combustion device that is used for destroying organic compounds and does not extract energy in the form of steam or process heat.(k) “Process heater” 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.(L) “Process unit” means equipment assembled and connected by pipes or ducts to produce, as intermediates or final products, one or more of the chemicals in sub. (8) . A process unit can operate independently if supplied with suf ficient fuel or raw materials and sufficient product storage facilities. (m) “Product” means any compound or chemical listed in sub. (8)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.(n) “Recovery device” means an individual unit of equipment, suchas an absorber, carbon adsorber or condenser, capable of and used for the purposeof recovering chemicals for use,

reuse or sale. (o) “Recovery system” means an individual recovery device or series of such devices applied to the same vent stream.(p) “Total organic compounds” or “TOC” means those compounds measured according to the procedures in sub. (5) (b) 4. For the purposes of measuring molar composition as required in sub. (5) (e) 2. a. , hourly emissions rate as required in sub. (5) (e) 5. and (f) , and TOC concentration as required in sub. (6) (b) 4. and (g) 4. , those compounds which the department has determined do not contribute appreciably to the formation of ozone are to be excluded. The compounds to be excluded are identified in s. NR 400.02 (162)

.(q) “TRE index value” means a measure of supplemental total resource requirement per unit reduction of TO C 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 sub. (5) (e)

. (r) “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. (3) S TANDARDS.Each owner or operator of any affected facility shall comply with par. (a)

, (b)or (c) for each vent streamon and after the date on which the initial performance test required by s. NR 440.08 and sub. (5)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 theinitial startup, whichever date comes first. Each owner or operator shall either: (a) Reduce emission of TOC, less methane and ethane, by 98weight−percent or to a TOC, less methane and ethane, concentration of 20 ppmv, on a dry basis corrected to 3% oxygen, whichever is less stringent. If a boiler or process heater is used to comply with this paragraph, then the 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 s. NR 440.18 ; or (c) Maintain a TRE index value greater than 1.0 without use of VOC emission control devices. (4) 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 sub. (3)shall install, calibrate, maintain and operate according to manufacturer’s specifications the following equipment:1. A temperature monitoring device equipped with a continuous recorder and having an accuracy of  1% of the temperature being monitored expressed in degrees Celsius or  0.5 ° C, whichever is greater. a. Where an incinerator other than a catalytic incinerator is used, a temperature monitoring device shall be installed in the firebox.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. A flow indicator that provides a record of vent stream flow to the incinerator at least once every hour for each af fected 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 sub. (3) (b)shall install, calibrate, maintain and operate according to manufacturer’s specifications the following equipment: 1. 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 af fected facility. The flow indicator 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 sub. (3) (a)shall install, calibrate, maintain and operate according to the manufacturer’s specifications the following equipment: 1. A flow indicator that provides a record of vent stream flow to the boiler or process heater at least once every hour for each af fected facility. The flow indicator shall be installed in the vent stream from each distillation unit within an affected facility437 NR 440.686 DEPARTMENT OF NATURAL RESOURCES

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### Register, May 2008, No. 629 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% 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. (d) The owner or operator of an affected facility that uses a boiler or process heater to comply with sub. (3) (a)shall monitor and record the periods of operation of the boiler or process heater if the design heat input capacity of the boiler or process heater is 44 MW (150 million Btu/hr) or greater. The records shall be readily available for inspection. (e) The owner or operator of an affected facility that seeks to comply with the TRE index value limit specified under sub. (3) (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 department:1. Where an absorber is the final recovery device in the recovery system:a. A scrubbing liquid temperature monitoring device having an accuracy of  1% 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 witha continuous recorder; orb. An organic monitoring device used to indicate the concentration level of or ganic compounds exiting the recovery device based on a detection principle such as infrared, photoionization or thermal conductivity, each quipped with a continuous recorder.2. Where a condenser is the final recovery device in the recovery system:a. The condenser exit (product side) temperature monitoring device equipped with a continuous recorder and having an accuracy of  1% of the temperature being monitored expressed in degrees Celsius or  0.5 ° C, whichever is greater; or b. 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: a. An integrating steam flow monitoring device having an accuracy of  10% and a carbon bed temperature monitoring device having an accuracy of  1% of the temperature being monitored expressed in degrees Celsius or  0.5 ° C, whichever is greater, both equipped with a continuous recorder; orb. An organic monitoring device used to indicate the concentration level of or ganic compounds exiting the recovery device based on a detection principle such as infra−red, photoionization or thermal conductivity, each equipped with a continuous recorder. (f) An owner or operator or an affected facility seeking to demonstrate c ompliance with the standards specified under sub. (3)with control devices other than incinerator, boiler, process heater or flare; or recovery device other than an absorber, condenser or carbon adsorber 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 specify appropriate monitoring procedures or requirements. (5) T EST METHODS AND PROCEDURES.(a) For the purpose of demonstrating compliance with sub. (3) , all af fected facilities shall be run at full operating conditions and flow rates during any performance test. (b) The following methods in Appendix A of 40 CFR part 60 , incorporated by reference in s. NR 440.17 , except as provided under s. NR 440.08 (2) , shall be used as reference methodsto determine compliance with the emission limit or percent reduction efficiency specified under sub. (3) (a)

.1. Method 1 or 1A, 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 (%O 2d) 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% O 2(C c) shall be completed using the following equation:

C c C TOC 17.9 20.9

 %0 2d where: C cis the concentration of TOC corrected to 3% O 2 , dry basis, ppm by volume C TOCis the concentration of TOC (minus methane and ethane), dry basis , ppm by volume %O 2d is the concentration of O 2 , 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 efficiency of the control device is to be determined. a. The sampling time for each run shall be 1 hour in which either an integrated sample or 4 grab samples shall be taken. If grab sampling is used then the samples shall be taken at 15−minute intervals. b. The emission reduction (R) of TOC (minus methane and ethane) shall be determined using the following equation:

R E i  E o E i  100

where: R is the emission reduction, percent by weight
E iis the mass rate of TOC entering the control device, kg/hr (lb/hr)
E ois the mass rate of TOC discharged to the atmosphere, kg/hr (lb/hr) c. The mass rates of TOC (Ei , Eo) shall be computed using the following equations

E i K 2 

#   n

j 1 C ij M ij 

#  Q i

E o K 2 

#   n

j 1 C oj M oj 

#  Q o

where: C ij and C oj are the concentration of sample component “j” of the gas stream at the inlet and outlet of the control device, respectively, dry basis, ppm by volume438 NR 440.686 WISCONSIN ADMINISTRATIVE CODE

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### Register, May 2008, No. 629 Mij and Moj are the molecular weight of sample component “j” of the gas stream at the inlet and outlet of the control device, respectively, g/g−mole (lb/lb−mole) Q iand Qoare the flow rate of gas stream at the inlet and outlet of the control device, respectively, dscm/min (dcsf/min)

K2is a constant, 2.494  10 −6(1/ppm) (g−mole/scm) (kg/g) (min/hr) for metric units, where standard temperature for (g−mole/scm) is 20 ° C, and 1.557 x 10 −7(1/ppm)(lb−mole/ scf)(min/hr) for English units, where standard temperature for (lb−mole/scf) is 68 F d. The TOC concentration (C TOC) is the sum of the individual components and shall be computed for each run using the following equation:

C TOC 

#  n

j 1 C j

where: C TOCis the concentration of TOC (minus methane and ethane), dry basis , ppm by volume C

j is the concentration of sample components “j”, dry basis, ppm by volume n is the number of components in the sample (c) 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 sub. (3) (a) , the requirement for an initial performance test is waived, in accordance with s. NR 440.08 (2)

. However, the department reserves the option to requiretesting at such other times as may be required. (d) When a flare is used to seek to comply with sub. (3) (b)

, the flare shall comply with the requirements of s. NR 440.18

. (e) The following test methods in Appendix A of 40 CFR part 60 , incorporated by reference in s. NR 440.17 , except as provided under s. NR 440.08 (2) , shall be used for determining the net heating value of the gas combusted to determine compliance under sub. (3) (b)and for determining the process vent stream TRE index value to determine compliance under sub. (3) (c)

.1. a. Method 1 or 1A, as appropriate, shall be used for selection of the sampling site. The sampling site for the vent stream flow rate and molar composition determination prescribed in subds. 2. and 3. shall be, except for the situations outlined in subd. 1. b. , prior to the inlet of any control device, prior to any post−distillation 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 10 centimeters (4 inches) in diameter. b. If any gas stream other than the distillation vent stream from the af fected facility is normally conducted through the final
recovery device then all of the following apply: 1) The sampling site for vent stream flow rate and molar composition shall be prior to the final recovery device and prior to the point at which the nondistillation stream is introduced. 2) 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 at the outlet of the final recovery device. 3) This ef ficiency 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 subds. 4. and 5. 2. The molar composition of the process vent stream shall be determined as follows:a. Method 18 to measure the concentration of TOC including those containing halogens. b. ASTM D1946−90 (reapproved 1994), incorporated by reference in s. NR 440.17 (2) (a)24., to measure the concentration of carbon monoxide and hydrogen. c. 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 following equation:

H T K 1 

#   n

j 1 Cj Hj 

# 

where: H Tis the net heating value of the sample, MJ/scm (Btu/scf),where the net enthalpy per mole of vent stream is based on combustion at 25 ° C and 760 mm Hg (77 F and 30 in. Hg), but the standard temperature for determining the volume corresponding to one mole is 20 ° C (68 F) K 1 is a constant, 1.740 x 10 −7(1/ppm)(g−mole/scm)(MJ/ kcal) for metric units where standard temperature for (g−mole/ scm) is 20 C, and 1.03 x 10−11 (1/ppm)(lb−mole/scf)(Btu/kcal) for English units where standard temperature for (lb−mole/scf) is 68 F C

j is the concentration on a wet basis of compound j in ppm, as measured for or ganics by Method 18 and measured for hydrogen and carbon monoxide by ASTM D1946−90 (reapproved 1994), incorporated by reference in s. NR 440.17 (2) (a)24., as indicated in subd. 2. H

j is the net heat of combustion of compound j, kcal/g−mole (kcal/lb−mole), based on combustion at 25 C and 760 mm Hg (77 F and 30 in Hg). The heats of combustion of vent stream components would be required to be determined using ASTM D2382−88 or D4809−95, incorporated by reference as specified in s. NR 440.17 (2) (a)30. and 61., if published values are not available or cannot be calculated. The heats of combustion of vent stream components wouldbe required to be determined using ASTM D2382−76, incorporated by reference as specified in s. NR 440.17 , 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:

E TOC K 2 

#   n

j 1 Cj Mj 

#  Q s

where: E TOCis the emission rate of TOC in the sample, kg/hr (lb/hr)

K2is the constant, 2.494  10 −6(1/ppm)(g−mole/scm) (kg/g) (min/hr) for metric units, where standard temperature for (g−mole/scm) is 20 C, and 1.557 x 10 −7(1/ppm)(lb−mole/ scf)(min/hr) for English units, where standard temperature for (lb−mole/scf) is 68 F C

j is the concentration on a wet basis of compound j in ppm as measured by Method 18 as indicated in subd. 2. M

j is the molecular weight of sample j, g/g−mole (lb/lb− mole) Q sis the vent stream flow rate, scm/min (scf/hr), at a temperature of 20 C (68 F) 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. (f) For purpose of complying with sub. (3) (c) , the owner or operator of a facility affected by this section shall calculate theTRE index value of the vent stream using the equation for incineration in subd. 1. for halogenated vent streams. The owner or operator of an affected facility with a nonhalogenated vent439 NR 440.686 DEPARTMENT OF NATURAL RESOURCES

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### Register, May 2008, No. 629 stream shall determine the TRE index value by calculating values using both the incinerator equation in subd. 1. and the flare equation in subd. 2. and selecting the lower of the 2 values. 1. The equation for calculating the TRE index value of a vent stream controlled by an incinerator is as follows:

TRE 1 E TOC a b  Q s  0.88 c  Q s  d Q s   H T  e  Q s  0.88  H T  0.88 f  Y s  0.5
a. Where for a vent stream flow rate that is greater than or equal to 14.2 scm/min (501 scf/min) at a standard temperature of 20 C (68 F): TRE is the TRE index value Q sis the vent stream flow rate scm/min (scf/min), at a standard temperature of 20 ° C (68 F)
H Tis the vent stream net heating value MJ/scm (Btu/scf), where the net enthalpy per mole of vent stream is based on combustion at 25 ° C and 760 mm Hg (68 F and 30 in Hg), but the standard temperature for determining the volume corresponding to one mole is 20 ° C (68 F), as in the definition of Q s Y s= Qsfor all vent stream categories listed in T able 1 except for Category E vent streams where Ys= (Q s ) (HT)/3.6 for metric units and Y s= (Q s )(HT)/97 for English units.
E TOCis the hourly emissions of TOC, kg/hr (lb/hr) a,b,c,d,e and f are coefficients. The set of coefficients that apply to a vent stream shall be obtained from Table 1.

Table 1. Distillation NSPS TRE Coefficients for Vent Streams Controlled By An Incinerator
Design Category A1. For Halogenated Process Vent Streams,
If 0 Net Heating Value (MJ/scm) 3.5 Or If 0 Net Heating Value (Btu/scf) 94: Q s= Vent Stream Flow Rate scm/min (scf/min) a b c d e f 1) 14.2 Q s 18.8 (501 Qs 664) 19.18370 (42.29238) 0.27580 (0.017220) 0.75762 (0.072549) −0.13064 (−0.00030361) 0 (0) 0.01025 (0.003803)

2) 18.8 < Q s 699 (664 < Qs 24,700) 20.00563 (44.10441) 0.27580 (0.017220) 0.30387 (0.029098) −0.13064 (−0.00030361) 0 (0) 0.01025 (0.003803)

3) 699 < Q s 1400 (24,700 < Qs 49,000) 39.87022 (87.89789) 0.29973 (0.018714) 0.30387 (0.029098) −0.13064 (−0.00030361) 0 (0) 0.01449 (0.005376)

4) 1400 < Q s 2100 (49,000 < Qs 74000) 59.73481 (131.6914) 0.31467 (0.019647) 0.30387 (0.029098) −0.13064 (−0.00030361) 0 (0) 0.01775 (0.006585)

5) 2100 < Q s 2800 (74,000 < Qs 99,000) 79.59941 (175.4849) 0.32572 (0.020337) 0.30387 (0.029098) −0.13064 (−0.00030361) 0 (0) 0.02049 (0.007602)

6) 2800 < Q s 3500 (99,000 < Qs 120,000) 99.46400 (219.2783) 0.33456 (0.020888) 0.30387 (0.029098) −0.13064 (−0.00030361) 0 (0) 0.02291 (0.008500)

Design Category A2. For Halogenated Process Vent Streams, If Net Heating Value 3.5 MJ/scm Or If Net Heating Value > 94 (Btu/scf): Q s= Vent Stream Flow Rate scm/min (scf/min) a b c d e f 7) 14.2 Q s 18.8 (501 Qs 664) 18.84466 (41.54494) 0.26742 (0.016696) −0.20044 (−0.019194) 0 (0) 0 (0) 0.01025 (0.003803)
8) 18.8 < Q s 699 (664 < Qs 24,700) 19.66658 (43.35694) 0.26742 (0.016696) −0.25332 (−0.024258) 0 (0) 0 (0) 0.01025 (0.003803)
9) 699 < Q s 1400 (24,700 < Qs 49,000) 39.19213 (86.40297) 0.29062 (0.018145) −0.25332 (−0.024258) 0 (0) 0 (0) 0.01449 (0.005376)
10) 1400 < Q s 2100 (49,000 < Qs 74000) 58.71768 (129.4490) 0.30511 (0.019050) −0.25332 (−0.024258) 0 (0) 0 (0) 0.01775 (0.006585)
11) 2100 < Q s 2800 (74,000 < Qs 99,000) 78.24323 (172.4950) 0.31582 (0.019718) −0.25332 (−0.024258) 0 (0) 0 (0) 0.02049 (0.007602)
12) 2800 < Q s 3500 (99,000 < Qs =120,000) 97.76879 (215.5411) 0.32439 (0.020253) −0.25332 (−0.024258) 0 (0) 0 (0) 0.02291 (0.008500)
Design Category B. For Nonhalogenated Process Vent Streams,
If 0 Net Heating Value (MJ/scm) 0.48 Or If 0 Net Heating Value (Btu/scf) 13: Q s= Vent Stream Flow Rate scm/min (scf/min) a b c d e f 13) 14.2 Q s 1340 (501 Qs 47,300) 8.54245 (18.83268) 0.10555 (0.0065901) 0.09030 (0.008647) −0.17109 (−0.00039762) 0 (0) 0.01025 (0.003803)
14) 1340 < Q s 2690 (47,300 < Qs 95,000) 16.94386 (37.35443) 0.11470 (0.0071614) 0.09030 (0.008647) −0.17109 (−0.00039762) 0 (0) 0.01449 (0.005376)
15) 2690 < Q s 4040 (95,000 < Qs 143,000) 25.34528 (55.87620) 0.12042 (0.0075185) 0.09030 (0.008647) −0.17109 (−0.00039762) 0 (0) 0.01775 (0.00658)
16) 14.2 Q s 1340 (501 Qs 47,300) 9.25233 (20.39769) 0.06105 (0.003812) 0.31937 (0.030582) −0.16181 (−0.00037605) 0 (0) 0.01025 (0.003803)440 NR 440.686 WISCONSIN ADMINISTRATIVE CODE

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### Register, May 2008, No. 629 Table 1. (Continued) Distillation NSPS TRE Coefficients for Vent Streams Controlled By An Incinerator (continued)
Design Category C. For Nonhalogenated Process Vent Streams,If 0.48 < Net Heating Value (MJ/scm) 1.9 Or If 13 < Net Heating Value (Btu/scf) 51: Q s= Vent Stream Flow Rate scm/min (scf/min) a b c d e f 17) 1340 < Qs 2690 (47,300 < Qs 95,000) 18.36363 (40.48446) 0.06635 (0.004143) 0.31937 (0.030582) −0.16181 (−0.00037605) 0 (0) 0.01449 (0.005376)
18) 2690 < Q s 4040 (95,000 < Qs 143,000) 27.47492 (60.57121) 0.06965 (0.004349) 0.31937 (0.030582) −0.16181 (−0.00037605) 0 (0) 0.01775 (0.006585)

Design Category D. For Nonhalogenated Process Vent Streams, If 1.9 < Net Heating Value (MJ/scm) 3.6 Or If 51 < Net Heating Value (Btu/scf) 97: Q s= Vent Stream Flow Rate scm/min (scf/min) a b c d e f 19) 14.2 Q s 1180 (501 Qs 41,700) 6.67868 (14.72382) 0.06943 (0.004335) 0.02582 (0.002472) 0 (0) 0 (0) 0.01025 (0.003803)
20) 1180 < Q s 2370 (41,700 < Qs 83,700) 13.21633 (29.13672) 0.07546 (0.004711) 0.02582 (0.002472) 0 (0) 0 (0) 0.01449 (0.005376)
21) 2370 < Q s 3550 (83,700 < Qs 125,000) 19.75398 (43.54962) 0.07922 (0.004946) 0.02582 (0.002472) 0 (0) 0 (0) 0.01775 (0.00658)

Design Category E. For Nonhalogenated Process Vent Streams, If Net Heating Value > 3.6 MJ/scm Or If Net Heating Value > 97 Btu/scf):

Ys= Dilution Flow Rate (scm/ min) = (Q s) (H T)/3.6 (scf/min) = (Q s)(H T)/97 a b c d e f 22) 14.2 Y s 1180 (501 Ys 41,700) 6.67868 (14.72382) 0 (0) 0 (0) −0.00707 (−0.0000164) 0.02220 (0.0001174) 0.01025 (0.003803)
23) 1180 < Y s 2370 (41,700 < Ys 83,700) 13.21633 (29.13672) 0 (0) 0 (0) −0.00707 (−0.0000164) 0.02412 (0.0001276) 0.01449 (0.005376)
24) 2370 < Y s 3550 (83,700 < Ys 125,000) 19.75398 (43.54962) 0 (0) 0 (0) −0.00707 (−0.0000164) 0.02533 (0.0001340) 0.01775 (0.006585)

b. Where for a vent stream flow rate that is less than 14.2 scm/min (501 scf/min) at a standard temperature of 20 C (68 F): TRE is the TRE index value Q s= 14.2 scm/min (501 scf/min) H T= (FLOW)(HVAL)/Q s where the following inputs are used: FLOW is the vent stream flow rate (scm/min) (scf/min), at a standard temperature of 20 ° C (68 ° F) HVAL is the vent stream net heating value MJ/scm (Btu/scf), where the net enthalpy per mole of vent stream is based on combustion at 25 ° C and 760 mm Hg (77 F and 30 in Hg), but the standard temperature for determining the volume corresponding to one mole is 20 ° C (68 ° F) as in the definition of Q s Y sis equal to Q sfor all vent stream categories listed in T able 1 except for Category E vent streams, where Ys = Q s H T/3.6 for metric units and Y s= Q s H T/97 for English units. E TOCis the hourly emissions of TOC reported in kg/hr (lb/hr) a,b,c,d,e and f are coefficients. The set of coefficients that apply to a vent stream shall 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 1 E TOC [a(Q s ) b(Q s ) 0.8 c(Q s )(H T) d(E TOC ) e]

where: TRE is the TRE index value E TOCis the hourly emissions of TOC, kg/hr (lb/hr) Q sis the vent stream flow rate scm/min (scf/min), at a standard temperature of 20 ° C (68 ° F) H Tis the vent stream net heating value, MJ/scm (Btu/scf), where the net enthalpy per mole of vent stream is based on combustion at 25 ° C and 760 mm Hg (77 F and 30 in Hg), but the standard temperature for determining the volume corresponding to one mole is 20 ° C (68 F) as in the definition of Q s a,b,c,d and e are coefficients. The set of coefficients that apply to a vent stream shall be obtained from Table 2.

Table 2. − Distillation NSPS TRE Coefficients for Vent Streams Controlled by a Flare

a b c d e

a. HT< 11.2 MJ/scm (HT < 301 Btu/scf) 2.25 (0.140) 0.288 (0.0367) −0.193 (−0.000448) −0.0051 (−0.0051) 2.08 (4.59)

b. HT  11.2 MJ/scm . . . . . . . . . . . . . . (HT  301 Btu/scf) 0.309 (0.0193) 0.0619 (0.00788) −0.0043 (−0.000010) −0.0034 (−0.0034) 2.08 (4.59)441 NR 440.686 DEPARTMENT OF NATURAL RESOURCES

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### Register, May 2008, No. 629

(g) Each owner or operator of an affected facility seeking to comply with sub. (1) (c) 4. or (3) (c)shall recalculate the TRE index value for that affected facility whenever process changesare made. Examples of process changes include changes in production capacity, feedstock type or catalyst type or wheneverthere 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 ef fects 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 department within one week of the recalculation and shall conduct a performance test according to the methods and procedures required by this subsection in order to determine compliance with sub. (3) (a) . Performance tests shall be conducted as soon as possible after the process change but 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 butgreater than 1.0, the owner or operator shall conduct a performance test in accordance with s. NR 440.08 and this subsection and shall comply with subs. (4)and (6)and this subsection. Performance tests shall be conducted as soon as possible after the process change but no later than 180 days from the time of the process change. (h) Any owner or operator subject to the provisions of this section seeking to demonstrate compliance with sub. (1) (c) 6. shall use Method 2, 2A, 2C or 2D as appropriate, for determination of volumetric flow rate. (6) REPORTING AND RECORDKEEPING REQUIREMENTS. (a) Each owner or operator subject to sub. (3)shall notify the department of the specific provisions of sub. (3)with which the owneror operator has elected to comply. Notification shall be submitted with the notification of initial startup required by s. NR 440.07 (1) (c) . If an owner or operator elects at a later date to use an alternative provision of sub. (3)with which he or she will comply, then the department shall be notified by the owner or operator within 90 days before implementing a change and,
upon implementing the change, a performance test shall be performed as specified by sub. (5)within 180 days. (b) Each owner or operator subject to the provisions of this section 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 s. NR 440.08 . 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 sub. (3) (a) , a report containing performance test data need not be submitted but a report containing the information in subd. 2. a. is required. The same data specified in this subsection shall be submitted in the reports of all subsequently required performance 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 section seeks to demonstrate compliance with sub. (3) (a) through use of either a thermal or catalytic incinerator: a. 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 minutesand averaged over the same time period of the performance testing and b. The percent reduction of TOC determined as specified in sub. (5) (b)achieved by the incinerator or the concentration of TOC (ppmv, by compound) determined as specified in sub. (5) (b)at the outlet of the control device on a dry basis corrected to 3% oxygen. 2. Where an owner or operator subject to the provisions of this section seeks to demonstrate compliance with sub. (3) (a) through use of a boiler or process heater: a. A description of the location at which the vent stream is introduced into the boiler or process heater, andb. 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 section seeks to demonstrate compliance with sub. (3) (b) through use of a smokeless flare, flare design, that is, steam−assisted, air−assisted or nonassisted, 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 recordsof all periods of operations during which the pilot flame is absent. 4 . Where an owner or operator subject to the provisions of this section seeks to demonstrate compliance with sub. (3) (c) :a. 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 department, and average exit temperature, ofthe 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; orb. Where a condenser is the final recovery device in the recovery system, the average exit (productside) 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 c. 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, and duration of the carbon bed steamingcycle, all measured while the vent stream is routed and constituted normally; or d. As an alternative to subd. 4. a.

, b. or c. , the concentration level or reading indicated by the organics monitoring device atthe outlet of the absorber, condenser or carbon adsorber, measured at least every 15 minutes and averaged over the same time period of the performancetesting while the vent stream is normally routed and constituted, ore. 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 section shall keep up−to−date, readily accessible continuous records of the equipment operating parameters specified to be monitored under sub. (4) (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 department may at any time requirea report of these data. Where a combustion device is used to comply with sub. (3) (a) , periods of operation duringwhich 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 sub. (3) (a)was determined. 2. For catalytic incinerators, all 3−hour periods of operation during which the average temperature of the vent stream imme-442 NR 440.686 WISCONSIN ADMINISTRATIVE CODE

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### Register, May 2008, No. 629 diately before the catalyst bed is more than 28 ° C (50 ° F) below the average combustion temperature during the most recent performance test at which compliance with sub. (3) (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% of the average temperature difference of the device during the most recent performance test at which compliance with sub. (3) (a)was determined. 3. All 3−hour periods of operation during which the average combustion temperature was more than 28 ° C (50 ° F) below theaverage combustion temperature during the most recent performance test at which compliance with sub. (3) (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 sub. (3) (a)

. (d) Each owner or operator subject to the provisions of this section shall keep up to date, readily accessible continuous records of the flow indication specified under sub. (4) (a) 2.

, (b) 2. and (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. (e) Each owner or operator subject to the provisions of this section who uses a boiler or process heater with a design heat input capacity of 44 MW (150 million Btu/hr) or greater to comply with sub. (3) (a)shall keep up−to− date, readily accessible records of all periods of operation of the boiler or process heater.

Note: 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 section shall keep up−to−date, readily accessible records of the flare pilot flame monitoring specified under sub. (4) (b) , as wellas 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 section shall keep up−to−date, readily accessible continuous records of the equipment operating parameters specified to be monitored under sub. (4) (e) , as well as up−to−date, readily accessible rec ords of all periods of operation during which the parameter boundaries established during the most recent performance test are exceeded. The department may at any time requirea report of these data. Where an owner or operator seeks to comply with sub. (3) (c) , periods of operation duringwhich 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: a. All 3−hour periods of operating du ring 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 b. 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 liquid saturation, is approved by the department, in which case the owner or operator 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 or ganic 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 (11 ° 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: a. All carbon bed regeneration cycles during which the total mass stream flow was more than 10% below the total mass
stream flow during the most recent performance test; orb. All carbon bed regeneration cycles during which the temperature of the carbon bed after regeneration, and after completion of any cooling cycle, was more than 10% greater than the carbon bed temperature (in degrees Celsius) during the most recent performance. 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 ofoperation during which the average organic compound concentration level or reading of or ganic compounds in the exhaust gases is more than 20% 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 tothe provisions of this section and seeking to demonstrate compliance with sub. (3) (c)shall keep up−to−date, readily accessible records of: 1. Any changes in production capacity, feedstock type or catalyst type or any replacement, removal or addition of recovery equipment or a distillation unit;2. Any recalculation of the TRE index value performed pursuant to sub. (5) (f) ; and 3. The results of any performance test performed pursuant to the methods and procedures required by sub. (5) (d)

. (i) Each owner or operator of an affected facility that seeks to comply with the requirements of this section by complying with the flow rate cutoff in sub. (1) (c) 6. shall keep up−to−date, readily accessible records to indicate that the vent stream flow rate is less than 0.008 scm/min (0.3 scf/min) and of any change in 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 section by complying with the design production capacity provision in sub. (1) (c) 5. shall keep up−to−date, readily accessible records of any changein 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 thissection is exempt from the quarterly reporting requirements contained in s. NR 440.07 (3)

.(L) Each owner or operator that seeks to comply with the requirements of this section by complying with the requirements of sub. (1) (c) 4.

, 5. or 6. or (3)shall submit to the department semiannual reports of the following recorded information. The initial report shall be submitted within 6 months after the initial startup date. 1. Exceedances of monitored parameters recorded under
pars. (c) and (g)

. 2. All periods recorded under par. (d)when the vent stream is diverted from the control device or has no flow rate. 3. All periods recorded under par. (e)when the boiler or process heater was not operating. 4. All periods recorded under par. (f)in which the pilot flame of the flare was absent.5. Any change in equipment or process operation that increases the operating vent stream flow rate above the low flow exemption level in sub. (1) (c) 6. , including a measurement of the443 NR 440.686 DEPARTMENT OF NATURAL RESOURCES

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### Register, May 2008, No. 629 new vent stream flow rate, as recorded under par. (i) . These shall be reported as soon as possible after the change and no later than 180 days after the change. These reports may be submitted either in conjunction with semiannual reports or as a single separate report. A performance test shall be completed with the same time period to verify the recalculated flow value and to obtain the vent stream characteristics of heating value and E TOC . The performance test is subject to the requirements of s. NR 440.08 . Unless the facility qualifies for an exemption under the low capacity exemption status in sub. (1) (c) 5. , the facility shall begin compliance with the requirements set forth in sub. (3)

.6. Any change in equipment or process operation, as recorded under par. (j) , that increases the design production capacity above the low capacity exemption level in sub. (1) (c) 5. and the new capacity resulting from the change for the distillation process unit containing the affected facility. These shall be reported as soon as possible after the change and no later than 180 days after the change. These reports may be submitted either in conjunction with semiannual reports or as a single separate report. A performance test shall be completed within the same time period to obtain the vent stream flow rate, heating value and E TOC . The performance test is subject to the requirements of s. NR 440.08 . The facility shall begin compliance with the requirements in sub. (1) (d)or (3) . If the facility chooses to comply with sub. (3) , the facility may qualify for an exemption in sub. (1) (c) 4. or 6. 7. Any recalculation of the TRE index value, as recorded under par. (h)

.(n) Each owner or operator that seeks to demonstrate compliance with sub. (1) (c) 5.shall submit to the department an initial report detailing the design production capacity of the process unit. (o) Each owner or operator thatseeks to demonstrate compliance with sub. (1) (c) 6.shall submit to the department an initial report including a flow rate measurement using the test methods specified in sub. (5)

. (p) The department will specify appropriate reporting and recordkeeping re quirements where the owner or operator of an affected facility complies with the standards specified under sub. (3)other than as provided under sub. (4) (a)to (d)

. (7) RECONSTRUCTION.(a) For purposes of this section, “fixed capital cost of the new components”, as used in s. NR 440.15 , 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 commended with 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. (8) C HEMICALS AFFECTED BY THIS SECTION.

Chemical Name CAS No.* 1. Acetaldehyde . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−07−0

2. Acetaldol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 107−89−1
3. Acetic acid . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 64−19−7 4. Acetic anhydride . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−24−7

5. Acetone . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 67−64−1 6. Acetone cyanohydrin . . . . . . . . . . . . . . . . . . . . . . . 75−86−5 7. Acetylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 74−86−2 8. Acrylic acid . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 79−10−7 9. Acrylonitrile . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 107−13−1 10. Adipic acid . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 124−04−9 11. Adiponitrile . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 111−69−3 12. Alcohols, C−11 or lower, mixtures . . . . . . . . . . . . . — Chemical Name CAS No.* 13. Alcohols, C−12 or higher, mixtures . . . . . . . . . . . .

— 14. Allyl chloride . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 107−05−1 15. Amylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 513−35−9 16. Amylenes, mixed . . . . . . . . . . . . . . . . . . . . . . . . . .

— 17. Aniline . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 62−53−3

18. Benzene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 71−43−2
19. Benzenesulfonic acid . . . . . . . . . . . . . . . . . . . . . . . 98−11−3

20. Benzenesulfonic acid C 10−16 −alkyl derivatives, sodium salts . . . . . . . . . . . . . . . . . . . . . . . . . . . . 68081−81−2 21. Benzoic acid, tech . . . . . . . . . . . . . . . . . . . . . . . . . . 65−85−0 22. Benzyl chloride . . . . . . . . . . . . . . . . . . . . . . . . . . . . 100−44−7 23. Biphenyl . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 92−52−4 24. Bisphenol A . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 80−05−7

25. Brometone . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 76−08−4 26. 1,3−Butadiene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 106−99−0
27. Butadiene and butene fractions . . . . . . . . . . . . . . . . —

28. n−Butane . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 106−97−8 29. 1,4−Butanediol . . . . . . . . . . . . . . . . . . . . . . . . . . . . 110−63−4 30. Butanes, mixed . . . . . . . . . . . . . . . . . . . . . . . . . . . . —

31. 1−Butene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 106−98−9

32. 2−Butene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 25167−67−3 33. Butenes, mixed . . . . . . . . . . . . . . . . . . . . . . . . . . . . — 34. n−Butyl acetate . . . . . . . . . . . . . . . . . . . . . . . . . . . . 123−86−4 35. Butyl acrylate . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 141−32−2 36. n−Butyl alcohol . . . . . . . . . . . . . . . . . . . . . . . . . . . 71−36−3 37. sec−Butyl alcohol . . . . . . . . . . . . . . . . . . . . . . . . . . 78−92−2 38. tert−Butyl alcohol . . . . . . . . . . . . . . . . . . . . . . . . . . 75−65−0 39. Butylbenzyl phthalate . . . . . . . . . . . . . . . . . . . . . . . 85−68−7 40. Butylene glycol . . . . . . . . . . . . . . . . . . . . . . . . . . . . 107−88−0 41. tert−Butyl hydroperoxide . . . . . . . . . . . . . . . . . . . . 75−91−2 42. 2−Butyne−1,4−diol . . . . . . . . . . . . . . . . . . . . . . . . . 110−65−6 43. Butyraldehyde . . . . . . . . . . . . . . . . . . . . . . . . . . . . 123−72−8 44. Butyric anhydride . . . . . . . . . . . . . . . . . . . . . . . . . . 106−31−0 45. Caprolactam . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 105−60−2
46. Carbon disulfide . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−15−0

47. Carbon tetrabromide . . . . . . . . . . . . . . . . . . . . . . . . 558−13−4

48. Carbon tetrachloride . . . . . . . . . . . . . . . . . . . . . . . . 56−23−5

49. Chlorobenzene . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−90−750. 2−Chloro−4−(ethylamino)−6−(isopropylamino)−s−triazine . . . . . . . . . . . . . . . . 1912−24−9
51. Chloroform . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 67−66−3 52. p−Chloronitrobenzene . . . . . . . . . . . . . . . . . . . . . . 100−00−5 53. Chloroprene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 126−99−8

54. Citric acid . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 77−92−9 55. Crotonaldehyde . . . . . . . . . . . . . . . . . . . . . . . . . . . 4170−30−0
56. Crotonic acid . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 3724−65−0

57. Cumene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 98−82−8 58. Cumene hydroperoxide . . . . . . . . . . . . . . . . . . . . . 80−15−9 59. Cyanuric chloride . . . . . . . . . . . . . . . . . . . . . . . . . . 108−77−0 60. Cyclohexane . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 110−82−7 61. Cyclohexane, oxidized . . . . . . . . . . . . . . . . . . . . . . 68512−15−2 62. Cyclohexanol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−93−0 63. Cyclohexanone . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−94−1 64. Cyclohexanone oxime . . . . . . . . . . . . . . . . . . . . . . 100−64−1 65. Cyclohexene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 110−83−8 66. 1,3−Cyclopentadiene . . . . . . . . . . . . . . . . . . . . . . . 542−92−7 67. Cyclopropane . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−19−4

68. Diacetone alcohol . . . . . . . . . . . . . . . . . . . . . . . . . . 123−42−2
69. Dibutanized aromatic concentrate . . . . . . . . . . . . . . — 70. 1,4−Dichlorobutene . . . . . . . . . . . . . . . . . . . . . . . . 110−57−8444 NR 440.686 WISCONSIN ADMINISTRATIVE CODE

The Wisconsin Administrative Code on this web site is current through the last published Wisconsin Register . See also Are the Codes on this Website Official? 

### Register, May 2008, No. 629 Chemical Name CAS No.* 71. 3,4−Dichlor−1−butene . . . . . . . . . . . . . . . . . . . . . . 64037−54−3

72. Dichlorodifluoromethane . . . . . . . . . . . . . . . . . . . . 75−71−8 73. Dichlorodimethylsilane . . . . . . . . . . . . . . . . . . . . . . 75−78−5
74. Dichlorofluoromethane . . . . . . . . . . . . . . . . . . . . . . 75−43−4 75. 1,3−Dichlorohydrin . . . . . . . . . . . . . . . . . . . . . . . . 96−23−1

76. Diethanolamine . . . . . . . . . . . . . . . . . . . . . . . . . . . . 111−42−2 77. Diethylbenzene . . . . . . . . . . . . . . . . . . . . . . . . . . . . 25340−17−4 78. Diethylene glycol . . . . . . . . . . . . . . . . . . . . . . . . . . 111−46−6 79. Di−n−heptyl−n−nonyl undecyl phthalate . . . . . . . . 85−68−7 80. Di−isodecyl phthalate . . . . . . . . . . . . . . . . . . . . . . . 26761−40−0 81. Diisononyl phthalate . . . . . . . . . . . . . . . . . . . . . . . . 28553−12−0 82. Dimethylamine . . . . . . . . . . . . . . . . . . . . . . . . . . . . 124−40−3 83. Dimethyl terephthalate . . . . . . . . . . . . . . . . . . . . . . 120−61−6 84. 2,4−Dinitrotoluene . . . . . . . . . . . . . . . . . . . . . . . . . 121−14−2 85. 2,6−Dinitrotoluene . . . . . . . . . . . . . . . . . . . . . . . . . 606−20−2 86. Dioctyl phthalate . . . . . . . . . . . . . . . . . . . . . . . . . . . 117−81−7

87. Dodecene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 25378−22−7 88. Dodecylbenzene, non linear . . . . . . . . . . . . . . . . . . — 89. Dodecylbenzenesulfonic acid . . . . . . . . . . . . . . . . . 27176−87−0 90. Dodecylbenzenesulfonic acid, sodium salt . . . . . . . 25155−30−0 91. Epichlorohydrin . . . . . . . . . . . . . . . . . . . . . . . . . . . 106−89−8
92. Ethanol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 64−17−5
93. Ethanolamine . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 141−43−5 94. Ethyl acetate . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 141−78−6 95. Ethyl acrylate . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 140−88−5 96. Ethylbenzene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 100−41−4 97. Ethyl chloride . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−00−3 98. Ethyl cyanide . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 107−12−0 99. Ethylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 74−85−1 100. Ethylene dibromide . . . . . . . . . . . . . . . . . . . . . . . . 106−93−4 101. Ethylene dichloride . . . . . . . . . . . . . . . . . . . . . . . . . 107−06−2 102. Ethylene glycol . . . . . . . . . . . . . . . . . . . . . . . . . . . . 107−21−1 103. Ethylene glycol monobutyl . . . . . . . . . . . . . . . . . . . 111−76−2 104. Ethylene glycol monoethyl ether . . . . . . . . . . . . . . 110−80−5 105. Ethylene glycol monoethyl ether acetate . . . . . . . . 111−15−9 106. Ethylene glycol monomethyl ether . . . . . . . . . . . . . 109−86−4 107. Ethylene oxide . . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−21−8 108. 2−Ethylhexanal . . . . . . . . . . . . . . . . . . . . . . . . . . . . 26266−68−2 109. 2−Ethylhexyl alcohol . . . . . . . . . . . . . . . . . . . . . . . 104−76−7 110. (2−Ethylhexyl) amine . . . . . . . . . . . . . . . . . . . . . . . 104−75−6 111. Ethylmethylbenzene . . . . . . . . . . . . . . . . . . . . . . . . 25550−14−5 112. 6−Ethyl−1,2,3,4−tetrahydro−9,10−anthracenedione 15547−17−8 113. Formaldehyde . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 50−00−0 114. Glycerol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 56−81−5 115. n−Heptane . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 142−82−5 116. Heptenes, mixed . . . . . . . . . . . . . . . . . . . . . . . . . . . — 117. Hexadecyl chloride . . . . . . . . . . . . . . . . . . . . . . . . . — 118. Hexamethylene diamine . . . . . . . . . . . . . . . . . . . . . 124−09−4 119. Hexamethylene diamine adipate . . . . . . . . . . . . . . . 3323−53−3 120. Hexamethylenetetramine . . . . . . . . . . . . . . . . . . . . 100−97−0

121. Hexane . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 110−54−3
122. 2−Hexenedinitrile . . . . . . . . . . . . . . . . . . . . . . . . . . 13042−02−9
123. 3−Hexenedinitrile . . . . . . . . . . . . . . . . . . . . . . . . . . 1119−85−3 124. Hydrogen cyanide . . . . . . . . . . . . . . . . . . . . . . . . . . 74−90−8

125. Isobutane . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−28−5
126. Isobutanol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 78−83−1 127. Isobutylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 115−11−7 128. Isobutyraldehyde . . . . . . . . . . . . . . . . . . . . . . . . . . 78−84−2 129. Isodecyl alcohol . . . . . . . . . . . . . . . . . . . . . . . . . . . 25339−17−7 130. Isooctyl alcohol . . . . . . . . . . . . . . . . . . . . . . . . . . . 26952−21−6 Chemical Name CAS No.* 131. Isopentane . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 78−78−4 132. Isophthalic acid . . . . . . . . . . . . . . . . . . . . . . . . . . . . 121−91−5 133. Isoprene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 78−79−5 134. Isopropanol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 67−63−0

135. Ketene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 463−51−4 136. Linear alcohols, ethoxylated, mixed . . . . . . . . . . . . — 137. Linear alcohols, ethoxylated and sulfated, sodium salt, mixed . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .

— 138. Linear alcohols, sulfated, sodium salt, mixed . . . . . — 139. Linear alkylbenzene . . . . . . . . . . . . . . . . . . . . . . . . 123−01−3 140. Magnesium acetate . . . . . . . . . . . . . . . . . . . . . . . . . 142−72−3 141. Maleic anhydride . . . . . . . . . . . . . . . . . . . . . . . . . . 108−31−6

142. Melamine . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−78−1 143. Mesityl oxide . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 141−79−7 144. Methacrylonitrile . . . . . . . . . . . . . . . . . . . . . . . . . . 126−98−7
145. Methanol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 67−56−1 146. Methylamine . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 74−89−5 147. ar−Methylbenzenediamine . . . . . . . . . . . . . . . . . . . 25376−45−8 148. Methyl chloride . . . . . . . . . . . . . . . . . . . . . . . . . . . 74−87−3 149. Methylene chloride . . . . . . . . . . . . . . . . . . . . . . . . . 75−09−2 150. Methyl ethyl ketone . . . . . . . . . . . . . . . . . . . . . . . . 78−93−3 151. Methyl iodide . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 74−88−4 152. Methyl isobutyl ketone . . . . . . . . . . . . . . . . . . . . . . 108−10−1 153. Methyl methacrylate . . . . . . . . . . . . . . . . . . . . . . . . 80−62−6 154. 2−Methylpentane . . . . . . . . . . . . . . . . . . . . . . . . . . 107−83−5 155. 1−Methyl−2−pyrrolidone . . . . . . . . . . . . . . . . . . . . 872−50−4 156. Methyl tert−butyl ether . . . . . . . . . . . . . . . . . . . . . . — 157. Naphthalen . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 91−20−3
158. Nitrobenzene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 98−95−3

159. 1−Nonene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 27215−95−8 160. Nonyl alcohol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 143−08−8 161. Nonylphenol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 25154−52−3 162. Nonylphenol, ethoxylated . . . . . . . . . . . . . . . . . . . . 9016−45−9

163. Octene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 25377−83−7 164. Oil−soluble petroleum sulfonate, calcium salt . . . . . — 165. Oil−soluble petroleum sulfonate, sodium salt . . . . . — 166. Pentaerythritol . . . . . . . . . . . . . . . . . . . . . . . . . . . . 115−77−5

167. n−Pentane . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 109−66−0
168. 3−Pentenenitrile . . . . . . . . . . . . . . . . . . . . . . . . . . . 4635−87−4 169. Pentenes, mixed . . . . . . . . . . . . . . . . . . . . . . . . . . . 109−67−1 170. Perchloroethylene . . . . . . . . . . . . . . . . . . . . . . . . . . 127−18−4
171. Phenol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−95−2 172. 1−Phenylethyl hydroperoxide . . . . . . . . . . . . . . . . . 3071−32−7 173. Phenylpropane . . . . . . . . . . . . . . . . . . . . . . . . . . . . 103−65−1 174. Phosgene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−44−5 175. Phthalic anhydride . . . . . . . . . . . . . . . . . . . . . . . . . 85−44−9 176. Propane . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 74−98−6 177. Propionaldehyde . . . . . . . . . . . . . . . . . . . . . . . . . . . 123−38−6 178. Propionic acid . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 79−09−4 179. Propyl alcohol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 71−23−8 180. Propylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 115−07−1 181. Propylene chlorohydrin . . . . . . . . . . . . . . . . . . . . . 78−89−7 182. Propylene glycol . . . . . . . . . . . . . . . . . . . . . . . . . . . 57−55−6 183. Propylene oxide . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−56−9 184. Propyl alcohol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 71−23−8 185. Propylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 115−07−1 186. Sodium cyanide . . . . . . . . . . . . . . . . . . . . . . . . . . . 143−33−9
187. Sorbitol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 50−70−4 188. Styrene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 100−42−5 189. Terephthalic acid . . . . . . . . . . . . . . . . . . . . . . . . . . . 100−21−0445 NR 440.688 DEPARTMENT OF NATURAL RESOURCES

The Wisconsin Administrative Code on this web site is current through the last published Wisconsin Register . See also Are the Codes on this Website Official? 

### Register, May 2008, No. 629 Chemical Name CAS No.* 190. 1,1,2,2−Tetrachloroethane . . . . . . . . . . . . . . . . . . . 79−34−5 191. Tetraethyl lead . . . . . . . . . . . . . . . . . . . . . . . . . . . . 78−00−2 192. Tetrahydrofuran . . . . . . . . . . . . . . . . . . . . . . . . . . . 109−99−9 193. Tetra (methyl−ethyl) lead . . . . . . . . . . . . . . . . . . . . — 194. Tetramethyl lead . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−74−1
195. Toluene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−88−3 196. Toluene−2,4−diamine . . . . . . . . . . . . . . . . . . . . . . . 95−80−7197. Toluene−2,4 (and 2,6)−diisocyanate (80/20 mixture) . . . . . . . . . . 26471−62−5

198. Tribromomethane . . . . . . . . . . . . . . . . . . . . . . . . . . 75−25−2 199. 1,1,1−Trichloroethane . . . . . . . . . . . . . . . . . . . . . . . 71−55−6 200. 1,1,2−Trichloroethane . . . . . . . . . . . . . . . . . . . . . . . 79−00−5 201. Trichloroethylene . . . . . . . . . . . . . . . . . . . . . . . . . . 79−01−6
202. Trichlorofluoromethane . . . . . . . . . . . . . . . . . . . . . 75−89−4 203. 1,1,2−Trichloro−1,2,2−trifluoroethane . . . . . . . . . . 76−13−1
204. Triethanolamine . . . . . . . . . . . . . . . . . . . . . . . . . . . 102−71−6 205. Triethylene glycol . . . . . . . . . . . . . . . . . . . . . . . . . . 112−27−67 206. Vinyl acetate . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−05−4 207. Vinyl chloride . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−01−4 208. Vinylidene chloride . . . . . . . . . . . . . . . . . . . . . . . . . 75−35−4 209. m−Xylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−38−3 210. o−Xylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 95−47−6 211. p−Xylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 106−42−3 212. Xylenes, mixed . . . . . . . . . . . . . . . . . . . . . . . . . . . . 1330−20−7 213. m−Xylenol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 576−26−1
*CAS numbers refer to the Chemical Abstracts Service Registry numbers assigned to specifi c chemicals, isomers or mixtures of chemicals. 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 listed, whether CAS numbers have been assigned or not.

History: Cr. Register, July, 1993, No. 451 , eff. 8−1−93; am. (5) (e) 1. a., b., (8), Register, December, 1995, No. 480 , eff. 1−1−96 ; renum. (2) (a) (intro.) and 1. to 18. to be (2) (intro.) and (a) to (r), am. (2) (p), Register, November, 1999, No. 527 , eff. 12−1−99; CR 06−109 : cr. (1) (d), am. (4) (c) (intro.), (5) (b) 4. b. and c., (6) (g) (intro.), (i), (L) 5. and 6. and (8), renum. (4) (c) 3. to be (4) (d) and am., renum. (5) (b) 5., (c),(d), (e), (f) and (g) to be (5) (c), (d), (e), (f), (g) and (h) and am. (5) (e) 1., 2. b., 4. and 5. and (f) 1. a., b. and 2. Register May 2008 No. 629 , eff. 6−1−08; corrections in (1) (d) 2. and (2) (p) made under s. 13.92 (4) (b) 7. , Stats., Register May 2008 No. 629

. NR 440.688 Nonmetallic mineral processing plants. (1) APPLICABILITY AND DESIGNATION OF AFFECTED FA

CILITY.(a) Except as provided in pars. (am) and (b)to (d) , the provisions of this section are applicable to the following af fected facilities in fixed or portable nonmetallic mineral processing plants; each crusher, grinding mill, screening operation, bucket elevator, belt conveyor, bagging operation, storage bin, enclosed truck or railcar loading station. Also, crushers and grinding mills at hot mix asphalt facilities that reduce the size of nonmetallic minerals embedded in recycled asphalt pavement and subsequent affected facilities up to, but not including, the first storage silo or bin are subject to the provisions of this section. (am) The provisions of this section do not apply to facilities located in underground mines, or to stand−alone screening operations at plants without crushers or grinding mills. (b) An affected facility that is subject to the provisions of s. NR 440.22or 440.25 or that follows in the plant process any facility subject to the provisions of s. NR 440.22or 440.25 is not subject to the provisions of this section.(c) Facilities at the following plants are not subject to the provision of this section. 1. Fixed sand and gravel plants and crushed stone plants with capacities, as defined in sub. (2) , 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 sub. (2) , of 136 megagrams per hour (150 tons per hour) or less; and 3. Common clay plants and pumice plants with capacities, as defined in sub. (2) , 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 sub. (2)havingthe same function as the existing facility, the new facility is exempt from the provisions of subs. (3), (5)and (6)except as provided for in subd. 3.2. An owner or operator seeking to comply with this paragraph shall submit the information required in sub. (7) (a)

. 3. An owner or operator replacing all existing facilities in a production line with new facilities does not qualify for the exemption described in subd. 1. and shall comply with the provisions of subs. (3), (5)and (6). (e) An affected facility under par. (a)that commences construction, reconstruction, or modification after August 31, 1983 is subject to the requirements of this section. (2) D EFINITIONS.As used in this section, terms not defined in this subsection have the meanings given in s. NR 440.02

. (a) “Bagging operation” means the mechanical process by which bags are filled with nonmetallic minerals.(b) “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.(c) “Bucket elevator” means a conveying device of nonmetallic 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. (d) “Building” means any frame structure with a roof.(e) “Capacity” means the cumulative rated capacity of all initial crushers that are part of the plant.(f) “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 toa control device.(g) “Control device” means the air pollution control equipment used to reduce particulate matter emissions released to theatmosphere from one or more process operations at a nonmetallic mineral processing plant.(h) “Conveying system” means a device for transporting materials from one piece of equipment or location to another location within a plant. Conveying systems include but are not limited to the following: Feeders, belt conveyors, bucket elevators and pneumatic systems. (i) “Crusher” means a machine used to crush any nonmetallic minerals, and includes, but is not limited to the following types: jaw, gyratory, cone, roll, rod mill, hammermill and impactor. (j) “Enclosed truck or railcar loading station” means that portion of a nonmetallic mineral processing plant were nonmetallicminerals are loaded by an enclosed conveying system into enclosed trucks or railcars. (k) “Fixed plant” means any nonmetallic mineral processing plant at which the processing equipment specified in sub. (1) (a) is attached by a cable, chain, turnbuckle, bolt or other means (except electrical connections) to any anchor, slab, or structure including bedrock. (L) “Fugitive emission” means particulate matter that is not collected by a capture system and is released to the atmosphere at the point of generation. (m) “Grinding mill” means a machine used for the wet or dryfine crushing of any nonmetallic mineral. Grinding mills include, but are not limited to, the following types: hammer, roller, rod, pebble and ball, and fluid energy. The grinding mill includes the air conveying system, air separator, or air classifier, where such systems are used.(n) “Initial crusher” means any crusher into which nonmetallic minerals can be fed without prior crushing in the plant.450−5 NR 440.705 DEPARTMENT OF NATURAL RESOURCES

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### Register, May 2008, No. 629 device is not replaced at the pre−determined interval specified in sub. (13) (a) 3. b. (f) If compliance with the provisions of this section is delayed pursuant to sub. (9) , the notification required under s. NR 440.07 (1) (d)shall include the estimated date of the next scheduled refinery or process unit shutdown after the date of notification andthe reason why compliance with the standards is technically impossible without a refinery or process unit shutdown.

History: Cr. Register, July, 1993, No. 451 , eff. 8−1−93; am. (1) (b), (15), (j) 1., Register, December, 1995, No. 480 , eff. 1−1−96; CR 06−109 : am. (2) (d), (11) (a) 2. and 3. and (13) (a) 1. and 2., renum. (13) (a) 3. to be (13) (a) (3) (intro.) and am., cr. (13) (a) 3. a. and b., (15) (j) 11. and 12. and (o) and (16) (e) 4., r. and recr. (15) (j) 2. Register May 2008 No. 629 , eff. 6−1−08.

NR 440.705 Volatile organic compound emissions from synthetic organic chemical manufacturing industry (SOCMI) reactor processes. (1) APPLICA

BILITY AND DESIGNATION OF AFFECTED FACILITY. (a) This section applies to each affected facility designated in par. (b)that is part of a process unit that produces any of the chemicals listed in sub. (8)as a product, co−product, by−product or intermediate except as provided in par. (c)

.(b) The affected facility is any of the following for which construction, modification or reconstruction commenced after June 29, 1990: 1. Each reactor process not discharging its vent stream into a recovery system. 2. Each combination of a reactor process and the recovery system into which its vent stream is dischar ged. 3. Each combination of 2 or more reactor processes and thecommon recovery system into which their vent streams are discharged. (c) Exemptions from the provisions of par. (a) are as follows: 1. Any reactor process that is designed and operated as a batch operation is not an af fected facility. 2. Each af fected facility that has a total resource effectiveness (TRE) index value greater than 8.0 is exempt from all provisions of this section except for subs. (3) (c)

, (5) (d)

, (e) and (f)and (6) (g)

, (L) 1. and 6. and (t)

. 3. Each af fected facility in a process unit with a total design capacity for all chemicals produced within that unit of less than one gigagram per year (1,100 tons per year) is exempt from allprovisions of this section except for the recordkeeping and reporting requirements in sub. (6) (i)

, (L) 5. and (n)

. 4. Each affected facility operated with a vent stream flow rate less than 0.011 scm/min is exempt from all provisions of this section except for the test method and procedure and the recordkeeping and reporting requirements in subs. (5) (g)and (6) (h)

, (L) 4. and (o)

. 5. If the vent stream from an affected facility is routed to a distillation unit subject to s. NR 440.686and has no other releases to the air except for a pressure relief valve, the facility is exempt from all provisions of this section except for sub. (6) (r)

. 6. Any reactor process operating as part of a process unit which produces beverage alcohols or which uses, contains and produces no VOC is not an affected facility. 7

. Any reactor process that is subject to the provisions of s. NR 440.647is not an affected facility. 8. Each affected facility operated with a concentration of total organic compounds (TOC), less methane and ethane, in the vent stream less than 300 ppmv, as measured by Method 18 in Appendix A of 40 CFR part 60 , incorporated by reference in s. NR 440.17 , or a concentration of TOC in the vent stream less than 150 ppmv, as measured by Method 25A in Appendix A of 40 CFR part 60 , incorporated by reference in s. NR 440.17 , is exempt from all provisions of this section except for the test method and procedure and the reporting and recordkeeping requirements in subs. (5) (h)and (6) (j)

, (L) 8. and (p)

.

Note: The intent of these standards is to minimize emissions of VOC through the application of best demonstrated technology (BDT). The numerical emission limits in these standards are expressed in terms of TOC, measured as TOC less methane and ethane. This emission limit reflects the performance of BDT. (d) 1. Owners or operators of process vents that are subject to this section may choose to comply with the provisions of 40 CFR part 65 , subpart D, as in effect on December 14, 2000, to satisfy the requirements of subs. (3)to (6) . The provisions of 40 CFR part 65 , subpart D, as in ef fect on December 14, 2000, also satisfy the criteria of par. (c) 2.

, 4. and 8. Other provisions applying to an owner or operator who chooses to comply with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, are provided in 40 CFR 65.1

. 2. Owners or operators who choose to comply with 40 CFR part 65 , subpart D, as in ef fect on December 14, 2000, shall also comply with ss. NR 440.01

, 440.02

, 440.05

, 440.06

, 440.07 (1) (a)

and (d)

, 440.14 and 440.15 for those process vents. All sections or subsections from ss. NR 440.01 to 440.19 not specified in this subdivision do not apply to owners or operators of process vents complying with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, except that provisions required to be met prior to implementing 40 CFR part 65 still apply. Owners or operators who choose to comply with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, shall comply with 40 CFR part 65 , subpart A. 3. Owners or operators who choose to comply with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, at initial startup shall comply with subds. 1. and 2. for each vent streamon and after the date on which the initial performance test is completed, but not later than 60 days after achieving the maximum production rate at which the af fected facility will be operated, or 180 days after the initial startup, whichever date comes first. 4. Each owner or operator subject to the provisions of this section that chooses to comply with 40 CFR part 65 , subpart D, as in effect on December 14, 2000, at initial startup shall notify the administrator of the specific provisions of 40 CFR 65.63 (a) (1), (2) or (3), as in ef fect on December 14, 2000, with which the

owner or operator has elected to comply. Notification shall be submitted with the notification of initial startup required by 40 CFR 65.5 (b). (2) D EFINITIONS.All terms not defined in this section have the meanings given in s. NR 440.02 . In this section:(a) “Batch operation” means any noncontinuous reactor process that is not characterized by steady state conditions and in which reactants are not added and products are not removed simultaneously.(b) “Boiler” means any enclosed combustion device that extracts useful energy in the form of steam and is not an incinerator.(c) “By compound” means by individual stream components, not carbon equivalents. (d) “Car−seal” means a seal that is placed on a device that is used to change the position of a valve, for example, from opened to closed, in such a way that the position of the valve cannot be changed without breaking the seal.(e) “Combustion device” means an individual unit of equipment, such as an incinerator, flare, boiler or process heater, used for combustion of a vent stream discharged from the process
vent. (f) “Continuousrecorder” means a data recording device recording an instantaneous data value at least once every 15 minutes.(g) “Flame zone” means the portion of the combustion chamber in a boiler occupied by the flame envelope. (h) “Flow indicator” means a device which indicates whether gas flow is present in a line.(i) “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. (j) “Incinerator” means an enclosed combustion device thatis used for destroying organic compounds. If there is energy recovery, the energy recovery section and the combustion cham-450−6 NR 440.705 WISCONSIN ADMINISTRATIVE CODE

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### Register, May 2008, No. 629 bers are not of integral design. That is, the energy recovery section and the combustion section are not physically formed into one manufactured or assembled unit but are joined by ducts or connections carrying flue gas. (k) “Primary fuel” means the fuel fired through a burner ora number of similar burners. The primary fuel provides the principal heat input to the device and the amount of fuel is suf ficient to sustain operation without the addition of other fuels.(L) “Process heater” means a device that transfers heat liberated by burning fuel directly to process streams or to heat transfer liquids other than water.(m) “Process unit” means equipment assembled and connected by pipes or ducts to produce as intermediates or final products one or more of the chemicals in sub. (8) . A process unit can operate independently if supplied with sufficient feed or raw materials and sufficient product storage facilities. (n) “Product” means any compound or chemical listed in sub. (8)which 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 andintermediates are considered to beproducts. (o) “Reactor processes” means 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.(p) “Recovery device” means an individual unit of equipment, suchas an absorber, carbon adsorber or condenser, capable of and used for the purposeof recovering chemicals for use,

reuse or sale. (q) “Recovery system” means an individual recovery device or series of recovery devices applied to the same vent stream.(r) “Relief valve” means a valve used only to release an unplanned, nonroutine dischar ge. A relief valve discharge results from an operator error, a malfunction such as a power failure or equipment failure or other unexpected cause that requires immediate venting of gas from process equipment in order to avoid safety hazards or equipment damage.(s) “Secondary fuel” means a fuel fired through a burner other than a primary fuel burner. The secondary fuel may providesupplementary heat in addition to the heat provided by the primary fuel.(t) “Total organic compounds” or “TOC” means those compounds measured according to the procedures in sub. (5) (b) 4. For the purposes of measuring molar composition as required in sub. (5) (d) 2. a. and b. , hourly emission rate as required in sub. (5) (d) 5. and (e) and TOC concentration as required in sub. (6) (b) 4.and (f) 4. , those compounds which the department has determined do not contribute appreciably to the formation of ozone are to be excluded. (u) “Total resource effectiveness” or “TRE index value”

means a measure of the supplemental total resource requirement per unit reduction of TOC associated with a vent stream from an affected reactor process facility based on vent stream flow rate,emission rate of TOC, net heating value and corrosion properties, whether or not the vent stream contains halogenated compounds as quantified by the equation given under sub. (5) (e)

. (v) “Vent stream” means any gas stream discharged directlyfrom a reactor process to the atmosphere or indirectly to the atmosphere after diversion through other process equipment. The
vent stream excludes relief valve discharges and equipment leaks. (3) S TANDARDS.Each owner or operator of any affected facility shall comply with par. (a)

, (b)or (c) for each vent streamon and after the date on which the initial performance test required by s. NR 440.08 and sub. (5)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 startup, whichever date comes first. Each owner or operator shall either: (a) Reduce emissions of TOC, less methane and ethane, by98 weight percent or to a TOC, less methane and ethane, concentration of 20 ppmv on a dry basis corrected to 3% oxygen, whichever is less stringent. If a boiler or process heater is used to comply with this paragraph, then the 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 s. NR 440.18 ; or (c) Maintain a TRE index value greater than 1.0 without use of a VOC emission control device. (4) 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 sub. (3) (a)shall install, calibrate, maintain and operate according to manufacturer’s specifications the following equipment:1. A temperature monitoring device equipped with a continuous recorder and having an accuracy of 1% of the temperature being monitored expressed in degrees Celsius or 0.5 ° C, whichever is greater. 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 in a position 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. A flow indicator that provides a record of vent stream flow diverted from being routed to the incinerator at least once every 15 minutes for each af fected facility, except as provided in subd. 2. b. a. The flow indicator shall be installed at the entrance to any bypass line that could divert the vent stream from being routed to the incinerator, resulting in its emission to the atmosphere.b. Where the bypass line valve is secured in the closed position with a car−seal or a lock−and−key type configuration, a flow indicator is not required. A visual inspection of the seal or closure mechanism shall be performed at least once every month to ensure that the valve is maintained in the closed position and the vent stream is not diverted through the bypass line. (b) The owner or operator of an affected facility that uses a flare to seek to comply with sub. (3) (b)shall install, calibrate, maintain and operate according to manufacturer’s specifications the following equipment: 1. A heat sensing device, such as an ultraviolet 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 diverted from being routed to the flare at least once every 15 minutes for each affected facility, except as provided in subd. 2. b. a. The flow indicator shall be installed at the entrance to any bypass line that could divert the vent stream from being routed to the flare, resulting in its emission to the atmosphere.b. Where the bypass line valve is secured in the closed position with a car−seal or a lock−and−key type configuration, a flow indicator is not required. A visual inspection of the seal or closure mechanism shall be performed at least once every month to ensure that the valve is maintained in the closed position and the vent stream is not diverted through the bypass line. (c) The owner or operator of an affected facility that uses a boiler or process heater to seek to comply with sub. (3) (a)shall install, calibrate, maintain and operate according to the manufacturer’s specifications the following equipment:450−7 NR 440.705 DEPARTMENT OF NATURAL RESOURCES

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### Register, May 2008, No. 629 1. A flow indicator that provides a record of vent stream flow diverted from beingrouted to the boiler or process heater at least once every 15 minutes for each affected facility, except as provided in subd. 1. b. a. The flow indicator shall be installed at the entrance to any bypass line that could divert the vent stream from being routedto the boiler or process heater, resulting in its emission to the atmosphere.b. Where the bypass line valve is secured in the closed position with a car−seal or a lock−and−key type configuration, a flow indicator is not required. A visual inspection of the seal or closure mechanism shall be performed at least once every month to ensure that the valve is maintained in the closed position and the vent stream is not diverted through the bypass line. 2. A temperature monitoring device in the firebox equipped with a continuous recorder and having an accuracy of 1% of the temperature being monitored 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) design heat input capacity. Any vent stream introduced with primary fuel into a boiler or
process heater is exempt from this requirement. (d) The owner or operator of an affected facility that seeks to demonstrate compliance with the TRE index value limit specified under sub. (3) (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 department:1. Where an absorber is the final recovery device in the recovery system:a. A scrubbing liquid temperature monitoring device having an accuracy of 1% 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 witha continuous recorder; orb. 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, photoionization or thermal conductivity, each equipped with a continuous recorder.2. Where a condenser is the final recovery device in the recovery system:a. A product side condenser exit temperature monitoring device equipped with a continuous recorder and having an accuracy of 1% of the temperature being monitored expressed in degrees Celsius or 0.5 ° C, whichever is greater; orb. An organic monitoring device used to indicate the concentration level of or ganic compounds exiting the recovery device based on a detection principle such as infrared, 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: a. An integrating steam flow monitoring device having an accuracy of 10% and a carbon bed temperature monitoring device having an accuracy of 1% of the temperature being monitored expressed in degrees Celsius or 0.5 ° C, whichever is greater, both equipped with a continuous recorder; orb. An organic monitoring device used to indicate the concentration level of or ganic compounds exiting the recovery device based on a detection principle such as infrared, photoionization or thermal conductivity, each equipped with a continuous recorder. (e) An owner or operator of an affected facility seeking to demonstrate c ompliance with the standards specified under sub. (3)with a control device other than an incinerator, boiler, process heater or flare, or a recovery device other than an absorber, condenser or carbon adsorber, 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 specify appropriate monitoring procedures or requirements. (5) T EST METHODS AND PROCEDURES.(a) For the purpose of demonstrating compliance with sub. (3) , all af fected facilities shall be run at full operating conditions and flow rates during any performance test. (b) The following methods in Appendix A of 40 CFR part 60 , incorporated by reference in s. NR 440.17 , except as provided under s. NR 440.08 (2) , shall be used as reference methodsto determine compliance with the emission limit or percent reduction efficiency specified under sub. (3) (a) :1. Method 1 or 1A, 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 3Bshall be used to determine the oxygen concentration (%O 2d) 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% O 2(C c) shall be computed using the following equation:

C c  C TOC 17.9 20.9

 %0 2d where: C cis the concentration of TOC corrected to 3% O2 , dry basis ppm by volume C TOCis the concentration of TOC minus methane and ethane, dry basis ppm by volume %O 2d is the concentration of O 2 , 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 efficiency of the control device is to be determined. a. The minimum sampling time for each run shall be one hour in which either an integrated sample or 4 grab samples shallbe taken. If grab sampling is used, then the samples shall be taken at approximately 15−minute intervals. b. The emission reduction (R) of TOC, minus methane and ethane, shall be determined using the following equation: where:

R  E i  E o E i  100 R is the emission reduction, percent by weight E iis the mass rate of TOC entering the control device, kg TOC/hr E ois the mass rate of TOC discharged to the atmosphere, kg TOC/hr c. The mass rates of TOC (E i , Eo) shall be computed using the following equations:

E i  K 2 

#  n

j  1 C ij M ij Q i

E o  K 2 

#  n

j  1 C oj M oj Q o450−8 NR 440.705 WISCONSIN ADMINISTRATIVE CODE

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### Register, May 2008, No. 629 where: C ij , C oj is the concentration of sample component “j” of thegas stream at the inlet and outlet of the control device, respectively, dry basis ppm by volume Mij , Moj is the molecular weight of sample component “j” of the gas stream at the inlet and outlet of the control device, respectively, g/g−mole (lb/lb−mole) Q i , Q ois the flow rate of gas stream at the inlet and outlet of the control device respectively, dscm/min (dscf/hr)

K2is a constant, 2.494  10−6(l/ppm) (g−mole/scm) (kg/g) (min/hr), where standard temperature for g−mole/scm is 20 ° C d. The TOC concentration (C TOC) is the sum of the individual components and shall be computed for each run using the following equation:

C TOC  

#  n

j  1 C j

where: C TOCis the concentration of TOC, minus methane and ethane, dry basis ppm by volume C

j is the concentration of sample components “j“, dry basis ppm by volume n is the number of components in the sample 5. The requirement for an initial performance test is waived in accordance with s. NR 440.08 (2)for the following: a. 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 compliance with sub. (3) (a)

. b. When a vent stream is introduced into a boiler or process heater with the primary fuel. c. The department reserves the option to require testing at such other times as may be required. 6. For purposes of complying with the 98 weight percent reduction in sub. (3) (a) , if the vent stream entering a boiler or process heater with a design capacity less than 44 MW (150 million Btu/hour) is introduced with the combustion air or as secondary fuel, the weight percent reduction of TOC, minus methane and ethane, across the combustion device shall be determined bycomparing the TOC, minus methane and ethane, in all combusted vent streams, primary fuels and secondary fuels with theTOC, minus methane and ethane, exiting the combustion device. (c) When a flare is used to seek to comply with sub. (3) (b)

, the flare shall comply with the requirements of s. NR 440.18

. (d) The following test methods in Appendix A of 40 CFR part 60 , incorporated by reference in s. NR 440.17 , except as provided under s. NR 440.08 (2) , shall be used for determining the net heating value of the gas combusted to determine compliance under sub. (3) (b)and for determining the process vent stream TRE index value to determine compliance under subs. (1) (c) 2. and (3) (c)

. 1. a. Method 1 or 1A, as appropriate, for selection of the sampling site. The sampling site for the vent stream flow rate and molar composition determination prescribed in subds. 2. and 3. shall be, except for the situations outlined in subd. 1. b. , prior to the inlet of any control device, prior to any postreactor dilution of the stream with air and prior to any postreactor introductionof halogenated compounds into the process vent stream. No traverse site selection method is needed for vents smaller than 4 inches in diameter.b. If any gas stream other than the reactor vent stream is normally conducte d through the final recovery device: 1) The sampling site for vent stream flow rate and molar composition shall be prior to the final recovery device and priorto the point at which any nonreactor stream or stream from a nonaffected reactor process is introduced. 2) 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 vent
stream and at the outlet of the final recovery device. 3) This efficiency of the final recovery device shall be applied to the TOC concentration measured prior to the final
recovery device and prior to the introduction of any nonreactor
stream or stream from a nonaf fected reactor process to determine the concentration of TOC in the reactor process vent stream from thefinal recovery device. This concentration of TOC is then used to perform thecalculations outlined in subds. 4. and 5. 2. The molar composition of the process vent stream shall be determined as follows:a. Method 18 to measure the concentration of TOC including those containing halogens. b. ASTM D1946−90 (reapproved 1994), incorporated by reference in s. NR 440.17 (2) (a)24., to measure the concentration of carbon monoxide and hydrogen. c. 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 following equation:

H T  K 1 

#  n

j  1 C j H j ( 1–B ws )

where: H Tis the 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 s(vent stream flow rate)

K 1 is a constant, 1.740  10 −7(l/ppm) (g−mole/scm) (MJ/ kcal), where standard temperature for (g−mole/scm) is 20 ° C C

j is the concentration on a dry basis of compound “j” in ppm as measured for organics by Method 18 and measured forhydrogen and carbon monoxide by ASTM D1946−90 (reapproved 1994), incorporated by reference in s. NR 440.17 (2) (a) 24., as indicated in subd. 2. H

j is the 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 D2382−88 or D4809−95, incorporated by reference in s. NR 440.17 (2) (a)30. and 61., if published values are not available or cannot becalculated B wsis the water vapor content of the vent stream, proportion by volume5. The emission rate of TOC in the vent stream shall be calculated using the following equation:

E TOC  K 2 

#  n

j  1 C j M j Q s

where: E TOC is the emission rate of TOC in the sample, kg/hr

K2is a constant, 2.494  10−6(l/ppm) (g−mole/scm) (kg/g) (min/hr), where standard temperature for (g−mole/scm) is 20 ° C C

j is the concentration on a dry basis of compound “j” in ppm as measured by Method 18 as indicated in subd. 2. M

j is the molecular weight of sample “j“, g/g−mole Q sis the vent stream flow rate (dscm/min) at a temperature of 20 ° C6. The total 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 18.450−9 NR 440.705 DEPARTMENT OF NATURAL RESOURCES

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(e) For purposes of complying with subs. (1) (c) 2. and (3) (c), the owner or operator of a facility affected by this section shall calculate the TRE index value of the vent stream using the equation for incineration in subd. 1. 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 subd. 1. and the flare equation in subd. 2. and selecting the lower of the 2 values. 1. The equation for calculating the TRE index value of a
vent stream controlled by an incinerator is as follows:

TRE  1 E TOC  a  b(Q s ) 0.88  c(Q s )  d(Q s )(H T)  e(Q s ) 0.88 (H T) 0.88  f(Y s ) 0.5 a. 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 is the TRE index value Q sis the vent stream flow rate (scm/min) at a standard temperature of 20 ° C H Tis the 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 in the definition of Q s Y sis Qsfor all vent stream categories listed in T able 1 except for Category E vent streams where Y s= (Q s) (HT)/3.6 E TOCis the hourly emissions of TOC reported in kg/hr a, b, c, d, e and f are coef ficients. The set of coef ficients that apply to a vent stream can be obtained from Table 1.

Table 1. − Total Resource Effectiveness Coefficients for Vent Streams Controlled by an Incinerator Subject to the New Source Performance Stand ards for Reacto r Processes

a b c d e f

Design Category A1. For Halogenated Process Vent Streams, If 0 Net Heating Value (MJ/scm) 3.5: Q sis the Vent Stream Flow Rate (scm/min)
1) 14.2 Q s 18.8 19.18370 0.27580 0.75762 −0.13064 0 0.01025
2) 18.8 <Q s 699 20.00563 0.27580 0.30387 −0.13064 0 0.01025
3) 699 <Q s 1,400 39.87022 0.29973 0.30387 −0.13064 0 0.01449
4) 1,400 Q s 2,100 59.73481 0.31467 0.30387 −0.13064 0 0.01775
5) 2,100 Q s 2,800 79.59941 0.32572 0.30387 −0.13064 0 0.02049
6) 2,800 Q s 3,500 99.46400 0.33456 0.30387 −0.13064 0 0.02291

Design Category A2. For Halogenated Process Vent Streams, If Net Heating Value (MJ/scm)>3.5: Q sis the Vent Stream Flow Rate (scm/min)
7) 14.2 Q s 18.8 18.84466 0.26742 −0.20044 0 0 0.01025
8) 18.8 Q s 699 19.66658 0.26742 −0.25332 0 0 0.01025
9) 699 Q s 1,400 39.19213 0.29062 −0.25332 0 0 0.01449
10) 1,400 Q s 2,100 58.71768 0.30511 −0.25332 0 0 0.01775
11) 2,100 Q s 2,800 78.24323 0.31582 −0.25332 0 0 0.02049
12) 2,800 Q s 3,500 97.76879 0.32439 −0.25332 0 0 0.02291

Design Category B. For Nonhalogenated Process Vent Streams, If 0 Net Heating Value (MJ/scm) 0.48: Q sis the Vent Stream Flow Rate (scm/min)
13) 14.2 Q s 1,340 8.54245 0.10555 0.09030 −0.17109 0 0.01025
14) 1,340 Q s 2,690 16.94386 0.11470 0.09030 −0.17109 0 0.01449
15) 2,690 Q s 4,040 25.34528 0.12042 0.09030 −0.17109 0 0.01775

Design Category C. For Nonhalogenated Process Vent Streams, If 0.48  Net Heating Value (MJ/scm) 1.9: Q sis the Vent Stream Flow Rate (scm/min)
16) 14.2 Q s 1,340 9.25233 0.06105 0.31937 −0.16181 0 0.01025
17) 1,340 Q s 2,690 18.36363 0.06635 0.31937 −0.16181 0 0.01449
18) 2,690 Q s 4,040 27.47492 0.06965 0.31937 −0.16181 0 0.01775

Design Category D. For Nonhalogenated Process Vent Streams, If 1.9  Net Heating Value (MJ/scm) 3.6: Q sis the Vent Stream Flow Rate (scm/min)
19) 14.2 Q s 1,180 6.67868 0.06943 0.02582 0 0 0.01025
20) 1,180 Q s 2,370 13.21633 0.07546 0.02582 0 0 0.01449
21) 2,370 Q s 3,550 19.75398 0.07922 0.02582 0 0 0.01755

Design Category E. For Nonhalogenated Process Vent Streams, If Net Heating Value (MJ/scm)>3.6: Ysis the Dilution Flow Rate (scm/min)=(Q s)(H T)/3.6
22) 14.2 Y s 1,180 6.67868 0 0 −0.00707 0.02220 0.01025
23) 1,180 Y s 2,370 13.21633 0 0 −0.00707 0.02412 0.01449
24) 2,370 Y s 3,550 19.75398 0 0 −0.00707 0.02533 0.01755450−10 NR 440.705 WISCONSIN ADMINISTRATIVE CODE

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### Register, May 2008, No. 629b. For a vent stream flow rate (scm/min) at a standard temperature of 20 ° C that is less than 14.2 scm/min: TRE is the TRE index value Q sis 14.2 scm/min H T= (FLOW) (HVAL)/14.2 where the following inputs are used: FLOW is the vent stream flow rate (scm/min) at a standard temperature of 20 ° C HVAL is the 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 in the definition of Q s Y sis 14.2 scm/min for all vent streams except for Category E vent streams where Ys= (14.2) (HT)/3.6 E TOCis the hourly emissions of TOC reported in kg/hr a, b, c, d, e and f are coef ficients. 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  1 E TOC 

###  a(Q s )  b(Q s ) 0.8  c(Q s )(H T)  d(E TOC )  e
where: TRE is the TRE index value E TOCis the hourly emission rate of TOC reported in kg/hr Q sis the vent stream flow rate (scm/min) at a standard temperature of 20 ° C H Tis the vent stream net heating value (MJ/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 s a, b, c, d and e are co efficients. The set of coefficients that apply to a vent stream can be obtained from Table 2.

Table 2. − Total Resource Effectiveness Coefficients for Vent Streams Controlled by a Flare Subject to the New Source Performance Stand ards for Reacto r Processes

a b c d e

a. H T 11.2 MJ/scm . . . . . . . . . . . 2.25 0.288 −0.193 −0.0051 2.08

b. H T 11.2 MJ/scm . . . . . . . . . . 0.309 0.0619 −0.0043 −0.0034 2.08

(f) Each owner or operator of an affected facility seeking to comply with sub. (1) (c) 2. or (3) (c)shall recalculate the TRE index value for that affected facility whenever process changesare made. Examples of process changes include changes in production capacity, feedstock type or catalyst type or wheneverthere 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 ef fects of the change on 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 department within one week of the recalculation and shall conduct a performance test according to the methods and procedures required by this subsection in order to determine compliance with sub. (3) (a)

or (b) . Performance tests shall be conducted as soon as possible after the process change but no later than 180 days from the time of the process change. 2. Where 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 s. NR 440.08and this subsection and shall comply with subs. (4)and (6)and this subsection. Performance tests shall 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 section seeking to demonstrate compliance with sub. (1) (c) 4. shall use Method 2, 2A, 2C or 2D of Appendix A to 40 CFR part 60 , incorporated by reference in s. NR 440.17 , for determination of volumetric flow rate. (h) Each owner or operator seeking to demonstrate that areactor process vent stream has a TOC concentration for compliance with the low concentration exemption in sub. (1) (c) 8. shall conduct an initial test to measure TOC concentration. 1. The sampling site shall be selected as specified in par. (d) 1. a.2. Method 18 or Method 25A of Appendix A of 40 CFR part 60 , incorporated by reference in s. NR 440.17 , shall be used to measure concentration.3. Where Method 18 is used to qualify for the low concentration exclusion in sub. (1) (c) 8. , the procedures in par. (b) 4. a. and d. shall be used tomeasure TOC concentration and the procedures of par. (b) 3. shall be used to correct the TOC concentration to 3% oxygen. To qualify for the exclusion, the results shall demonstrate that the concentration of TOC corrected to 3% oxygen is below 300 ppm by volume. 4. Where Method 25A is used, the following procedures shall be used to calculate ppm by volume TOC concentration corrected to 3% oxygen:a. Method 25A shall be used only if a single organic compound is greater than 50% of total TOC, by volume, in the reactor process vent stream. This c ompound shall be the principal organic compound. b. The principal organic compound may be determined byeither process knowledge or test data collected using an appropriate reference method. 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 reactor process vent stream conditions.c. The principal organic compound shall be used as the calibration gas for Method 25A. d. The span value for Method 25A shall be 300 ppmv. e. Use of Method 25A 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.f. The owner or operator shall demonstrate that the concentration of TOC, including methane and ethane, measured by Method 25A, corrected to 3% oxygen, is below 150 ppm by volume to qualify for the low concentration exclusion in sub. (1) (c) 8. g. The concentration of TOC shall be corrected to 3% oxygen using the procedures and equation in par. (b) 3. (6) REPORTING AND RECORDKEEPING REQUIREMENTS. (a) Each owner or operator subject to sub. (3)shall notify the department of the specific provisions of sub. (3) (a)

, (b)or (c) with which the owner or operator has elected to comply. Notification shall be submitted with the notification of initial startup required by s. NR 440.07 (1) (c) . If an owner or operator elects at a later date to use an alternative provision of sub. (3)with which he or she will comply, then the department 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 sub. (5)no later than 180 days from initial startup.450−11 NR 440.705 DEPARTMENT OF NATURAL RESOURCES

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(b) Each owner or operator subject to the provisions of this section 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 s. NR 440.08 . Where a boiler or process heater with a design heat input capacity of 44 MW (150 million Btu/ hour) or greater is used or where the reactor process vent stream is introduced as the primary fuel to any size boiler or process heater to comply with sub. (3) (a) , a report containing performance test data need not be submitted, but a report containing the information in par. (b) 2. a. is required. The same data specifiedin this subsection shall be submitted in the reports of all subsequently required performance tests where either the emission control ef ficiency of a combustion 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 section seeks to demonstrate compliance with sub. (3) (a) through use of either a thermal or catalytic incinerator: a. 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 minutesand averaged over the same time period of the performance testing, and b. The percent reduction of TOC determined as specified in sub. (5) (b)achieved by the incinerator or the concentration of TOC (ppmv, by compound) determined as specified in sub. (5) (b)at the outlet of the control device on a dry basis corrected to 3% oxygen. 2. Where an owner or operator subject to the provisions of this section seeks to demonstrate compliance with sub. (3) (a) through use of a boiler or process heater: a. A description of the location at which the vent stream is introduced into the boiler or process heater, andb. 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 section seeks to demonstrate compliance with sub. (3) (b) through use of a smokeless flare, flare design, for example, steam−assisted, air−assisted or nonassisted, all visible emission readings, heat content determinations, flowrate measurements and exit velocity determinations made during theperformance 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 section seeks to demonstrate compliance with sub. (3) (c) :a. 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 thedepartment, and average exit temperature of the absorbing liquid measured at least every 15 minutes and averaged over the same time period of the performance testing, with both measured while the vent stream is normally routed and constituted; orb. Where a condenser is the final recovery device in the recovery system, the average product side exit 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 c. 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 or full carbon bed cycle, temperature of the carb on bed after regeneration and within 15 minutes of completion of any cooling cycle and duration of the carbon bed steaming cycle with all measured while the vent stream is routed and constituted normally; or d. As an alternative to subd. 4. a.

, b. or c. , the concentration level or reading indicated by the organics monitoring device atthe outlet of the absorber, condenser or carbon adsorber measured at least every 15 minutes and averaged over the same time period of the performancetesting while the vent stream is normally routed and constituted.e. 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 section shall keep up to date, readily accessible continuous records of the equipment operating parameters specified to be monitored under sub. (4) (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 department may at any time require a report of these data. Where a combustion device is used to comply with sub. (3) (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 sub. (3) (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) belowthe average temperature of the vent stream during the most recent performance test at which compliance with sub. (3) (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% of the average temperature difference of the bed during the most recent performance test at which compliance with sub. (3) (a)was determined. 3. All 3−hour periods of operation during which the average combustion temperature was more than 28 ° C (50 ° F) below theaverage combustion temperature during the most recent performance test at which compliance with sub. (3) (a)was determined for boilers or process heaters with a design heat input capacity of less than 44 MW (150 million Btu/hr) where the vent stream is introduced with the combustion air or as a secondary fuel. 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 sub. (3) (a)

. (d) Each owner or operator subject to the provisions of this section shall keep records of the following: 1. Up to date, readily accessible continuous records of the flow indication specified under sub. (4) (a) 2. a.

, (b) 2. a. and (c) 1. a.as well as up to date, readily accessible records of all periodsand the duration when the vent stream is diverted from the control device. 2. Where a seal mechanism is used to comply with sub. (4) (a) 2. b.

, (b) 2. b. , and (c) 1. b. , a record of continuous flow is not required. In such cases the owner or operator shall keep up to date, readily accessible records of all monthly visual inspections of the seals as well as readily accessible records of all periods and the duration when the seal mechanism is broken, the bypass line valve position has changed, the serial number of the broken car− seal has changed or when the key for a lock−and−key type configuration has been checked out. (e) Each owner or operator subject to the provisions of thissection shall keep up to date, readily accessible continuous records of the flare pilot flame monitoring specified under sub. (4) (b)as well as up to date, readily accessible records of all periods of operations in which the pilot flame is absent.450−12 NR 440.705 WISCONSIN ADMINISTRATIVE CODE

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(f) Each owner or operator subject to the provisions of thissection shall keep up to date, readily accessible continuous records of the equipment operating parameters specified to be monitored under sub. (4) (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 department may at any time require a report of these data. Where an owner or operator seeks to comply with sub. (3) (c) , periods of operation during which the parameter boundaries esta blished 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 c ompound monitoring device is not used: a. 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 b. 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 liquid saturation, is approved by the department in which case the department 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 or ganic compound monitoring device is not used,all 3−hour periods of operation during which the average product side exit condenser operating temperature was more than 6 ° C (11 ° F) above the average product side exit operating temperature during the most recent performance test. 3. Where a carbon adsorber is the final recovery device in a system and where an or ganic compound monitoring device is not used: a. All carbon bed regeneration cycles during which the total mass steam flow was more than 10% below the total mass steam flow during the most recent performance test; orb. All carbon bed regeneration cycles during which the temperature of the carbon bed after regeneration and after completion of any cooling cycle was more than 10% or 5 ° C greater, whichever is less stringent, 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 ofoperation during which the average organic compound concentration level or reading of or ganic compounds in the exhaust gases is more than 20% greater than the exhaust gas organic compound concentration level or reading measured by the monitoring device during the most recent performance test. (g) Each owner or operator of an affected facility subject tothe provisions of this section and seeking to demonstrate compliance with sub. (3) (c)shall keep up to date, readily accessible records of: 1. Any changes in production capacity, feedstock type orcatalyst type or of any replacement, removal or addition of recovery equipment or reactors;2. Any recalculation of the TRE index value performed pursuant to sub. (5) (f) ; and 3. The results of any performance test performed pursuant to the methods and procedures required by sub. (5) (d)

. (h) Each owner or operator of an af fected facility that seeks to comply with the requirements of this section by complying with the flow rate cutoff in sub. (1) (c) 4. shall keep up to date, readily accessible records to indicate that the vent stream flow rate is less than 0.011 scm/min and of any change in equipment or process operation that increases the operating vent stream flow rate, including a measurement of the new vent stream flow
rate. (i) Each owner or operator of an affected facility that seeks to comply with the requirements of this section by complying with the design production capacity provision in sub. (1) (c) 3. 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. (j) Each owner or operator of an affected facility that seeks to comply with the requirements of this section by complying with the low concentration exemption in sub. (1) (c) 8.shall keep up to date, readily accessible records of any change in equipment or process operation that increases the concentration of the vent stream of the af fected facility. (k) Each owner or operator subject to the provisions of this section is exempt from the quarterly reporting requirements contained in s. NR 440.07 (3)

.(L) Each owner or operator that seeks to comply with the requirements of this section by complying with the requirements of sub. (1) (c) 2.

, 3. or 4. or (3)shall submit to the department semiannual reports of the following recorded information. The initial report shall be submitted within 6 months after the initial startup date. 1. Exceedances of monitored parameters recorded under
pars. (c)

, (f)and (g)

. 2. All periods and duration recorded under par. (d)when thevent stream is diverted from the control device to the atmosphere. 3. All periods recorded under par. (e) in which the pilot flame of the flare was absent.4. Any change in equipment or process operation that increases the operating vent stream flow rate above the low flow exemption level in sub. (1) (c) 4. , including a measurement of the new vent stream flow rate, as recorded under par. (h) . These shall be reported as soon as possible after the change and no later than 180 days after the change. These reports may be submitted either in conjunction with semiannual reports or as a single separate report. A performance test shall be completed within the same time period to verify the recalculated flow value and to obtain the
vent stream characteristics of heating value and ETOC . The performance test is subject to the requirements of s. NR 440.08

. Unless the facility qualifies for an exemption under any of the exemption provisions listed in sub. (1) (c) , except for the total resource ef fectiveness index greater than 8.0 exemption in sub. (1) (c) 2. , the facility shall begin compliance with the requirements in sub. (3)

.5. Any change in equipment or process operation as recorded under par. (i)that increases the design production capacity above the low capacity exemption level in sub. (1) (c) 3. andthe new capacity resulting from the change for the reactor process unit containing the affected facility. These shall be reported as soon as possible after the change and no later than 180 days after the change. These reports may be submitted either in conjunction with semiannualreports or as a single separate report. A performance test shall be completed within the same time period to obtain the vent stream flow rate, heating value and E TOC . The performance test is subject to the requirements of s. NR 440.08 . The facility shall begin compliance with the requirements in sub. (1) (d)or (3) . If the facility chooses to comply with sub. (3) , the facility may qualify for an exemption under sub. (1) (c) 2.

, 4. or 8. 6. Any recalculation of the TRE index value as recorded under par. (g)

. 7. All periods recorded under par. (d)in which the seal mechanism is broken or the by−pass line valve position has changed. A record of the serial number of the car−seal or a record450−13 NR 440.705 DEPARTMENT OF NATURAL RESOURCES

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### Register, May 2008, No. 629 to show that the key to unlock the bypass line valve was checked out shall be maintained to demonstrate the period, the duration and frequency in which the bypass line was operated.8. Any change in equipment or process operation that increases the vent stream concentration above the low concentration exemption level in sub. (1) (c) 8. , including a measurement of the new vent stream concentration as recorded under par. (j)

. These shall be reported as soon as possible after the change and no later than 180 days after the change. These reports may be submitted either in conjunction with semiannual reports or as a single separate report. If the vent stream concentration is above 300 ppmv as measured using Method 18 of Appendix A of 40 CFR part 60 , incorporated by reference in s. NR 440.17 (1) , or above 150 ppmv as measured using Method 25A of Appendix A of 40 CFR part 60 , incorporated by reference in s. NR 440.17 (1) , a performance test shall be completed within the same time period to obtain the vent stream flow rate, heating value and E TOC . The performance test is subject to the requirements of s. NR 440.08 . Unless the facility qualifies for an exemption under any of the exemption provisions listed in sub. (1) (c) , except for the TRE index greater than 8.0 exemption in sub. (1) (c) 2. , the facility shall begin compliance with the requirements in sub. (3)

. (n) Each owner or operator thatseeks to demonstrate compliance with sub. (1) (c) 3.shall submit to the department an initial report detailing the design production capacity of the process unit. (o) Each owner or operator thatseeks to demonstrate compliance with sub. (1) (c) 4.shall submit to the department an initial report including a flow rate measurement using the test methods specified in sub. (5)

.(p) Each owner or operator that seeks to demonstrate compliance with sub. (1) (c) 8.shall submit to the department an initial report including a concentration measurement using the test method specified in sub. (5)

. (q) The department shall specify appropriate reporting and recordkeeping requirements where the owner or operator of an affected facility complies with the standards specified under sub. (3)other than as provided under sub. (4) (a)

, (b)

, (c) and (d)

. (r) Each owner or operator whose reactor process vent stream is routed to a distillation unit subject to s. NR 440.686and who seeks to demonstrate compliance with sub. (1) (c) 5.shall submitto the department a process design description as part of the initial report. This process design description shall be retained for the life of the process. No other records or reports are required unless process changes are made.(s) Each owner or operator who seeks to demonstrate compliance with sub. (3) (a)or (b)using a control device shall maintain on file a schematic diagram of the affected vent streams, collection system, fuel systems, control devices and bypass systems as part of the initial report. This schematic diagram shall be retained for the life of the system.(t) Each owner or operator that seeks to demonstrate compliance with sub. (1) (c) 2. shall maintain a record of the initial
test for determining the total re source effectiveness index and the results of the initial total resource effectiveness index calculation. (7) RECONSTRUCTION.(a) For purposes of this section “fixed capital cost of the new components,” as used in s. NR 440.15 , 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 June 29, 1990. 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. (8) C HEMICALS AFFECTED BY THIS SECTION.

Chemical Name CAS No. 1 1. Acetaldehyde . . . . . . . . . . . . . . . . . . . . . . . . . 75−07−0

2. Acetic . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 64−19−7

3. Acetic . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−24−7

4. Acetone . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 67−64−1

5. Acetone . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−86−5 6. Acetylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . 74−86−2 7. Acrylic . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 79−10−7 8. Acrylonitrile . . . . . . . . . . . . . . . . . . . . . . . . . 107−13−1 9. Adipic . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 124−04−9 10. Adiponitrile . . . . . . . . . . . . . . . . . . . . . . . . . . 111−69−3 11. Alcohols, C−11 or lower, mixtures . . . . . . . . . 12. Alcohols, C−12 or higher, mixtures . . . . . . . . 13. Alcohols, C−12 or higher, unmixed . . . . . . . . 14. Allyl chloride . . . . . . . . . . . . . . . . . . . . . . . . . 107−05−1 15. Amylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . 513−35−9 16. Amylenes, mixed . . . . . . . . . . . . . . . . . . . . . .

17. Aniline . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 62−53−3

18. Benzene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 71−43−2
19. Benzenesulfonic acid . . . . . . . . . . . . . . . . . . . 98−11−3 20. Benzenesulfonic acid C−alkyl derivatives, sodium salts . . . . . . . . . . . . . . . . . . . . . . . . 68081−81−2

21. Benzyl chloride . . . . . . . . . . . . . . . . . . . . . . . . 100−44−7 22. Bisphenol A . . . . . . . . . . . . . . . . . . . . . . . . . . 80−05−7

23. Brometone . . . . . . . . . . . . . . . . . . . . . . . . . . . 76−08−4 24. 1,3−Butadiene . . . . . . . . . . . . . . . . . . . . . . . . 106−99−0

25. Butadiene and butene fractions . . . . . . . . . . . .

26. n−Butane . . . . . . . . . . . . . . . . . . . . . . . . . . . . 106−97−8 27. 1,4−Butanediol . . . . . . . . . . . . . . . . . . . . . . . . 110−63−4 28. Butanes, mixed . . . . . . . . . . . . . . . . . . . . . . .

29. 1−Butene . . . . . . . . . . . . . . . . . . . . . . . . . . . . 106−98−9

30. 2−Butene . . . . . . . . . . . . . . . . . . . . . . . . . . . . 25167−67−3 31. Butenes, mixed . . . . . . . . . . . . . . . . . . . . . . . . 32. n−Butyl acetate . . . . . . . . . . . . . . . . . . . . . . . . 123−86−4 33. Butyl acrylate . . . . . . . . . . . . . . . . . . . . . . . . . 141−32−2 34. n−Butyl alcohol . . . . . . . . . . . . . . . . . . . . . . . 71−36−3 35. sec−Butyl alcohol . . . . . . . . . . . . . . . . . . . . . . 78−92−2 36. tert−Butyl alcohol . . . . . . . . . . . . . . . . . . . . . 75−65−0 37. Butylbenzyl phthalate . . . . . . . . . . . . . . . . . . 85−68−7 38. tert−Butyl hydroperoxide . . . . . . . . . . . . . . . . 75−91−2 39. 2−Butyne−1,4−diol . . . . . . . . . . . . . . . . . . . . 110−65−6 40. Butyraldehyde . . . . . . . . . . . . . . . . . . . . . . . . 123−72−8 41. Butyric anhydride . . . . . . . . . . . . . . . . . . . . . 106−31−0 42. Caprolactam . . . . . . . . . . . . . . . . . . . . . . . . . . 105−60−2

43. Carbon disulfide . . . . . . . . . . . . . . . . . . . . . . 75−15−0

44. Carbon tetrachloride . . . . . . . . . . . . . . . . . . . 56−23−5

45. Chloroacetic acid . . . . . . . . . . . . . . . . . . . . . . 79−11−8

46. Chlorobenzene . . . . . . . . . . . . . . . . . . . . . . . . 108−90−7

47. Chlorodifluoromethane . . . . . . . . . . . . . . . . . 75−45−6

48. Chloroform . . . . . . . . . . . . . . . . . . . . . . . . . . 67−66−3 49. p−Chloronitrobenzene . . . . . . . . . . . . . . . . . . 100−00−5

50. Citric acid . . . . . . . . . . . . . . . . . . . . . . . . . . . 77−92−9

51. Cumene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 98−82−8 52. Cumene hydroperoxide . . . . . . . . . . . . . . . . . 80−15−9 53. Cyanuric chloride . . . . . . . . . . . . . . . . . . . . . 108−77−0 54. Cyclohexane . . . . . . . . . . . . . . . . . . . . . . . . . 110−82−7 55. Cyclohexane, oxidized . . . . . . . . . . . . . . . . . . 68512−15−2 56. Cyclohexanol . . . . . . . . . . . . . . . . . . . . . . . . . 108−93−0450−14 NR 440.705 WISCONSIN ADMINISTRATIVE CODE

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### Register, May 2008, No. 629 Chemical Name CAS No. 1 57. Cyclohexanone . . . . . . . . . . . . . . . . . . . . . . . 108−94−1 58. Cyclohexanone oxime . . . . . . . . . . . . . . . . . . 100−64−1 59. Cyclohexene . . . . . . . . . . . . . . . . . . . . . . . . . 110−83−8 60. Cyclopropane . . . . . . . . . . . . . . . . . . . . . . . . . 75−19−4

61. Diacetone alcohol . . . . . . . . . . . . . . . . . . . . . 123−42−2 62. 1,4−Dichlorobutene . . . . . . . . . . . . . . . . . . . . 110−57−6 63. 3,4−Dichloro−1−butene . . . . . . . . . . . . . . . . . 64037−54−3

64. Dichlorodifluoromethane . . . . . . . . . . . . . . . . 75−71−8 65. Dichlorodimethylsilane . . . . . . . . . . . . . . . . . 75−78−5

66. Dichlorofluoromethane . . . . . . . . . . . . . . . . . 75−43−4

67. Diethanolamine . . . . . . . . . . . . . . . . . . . . . . . 111−42−2 68. Diethylbenzene . . . . . . . . . . . . . . . . . . . . . . . 25340−17−4 69. Diethylene glycol . . . . . . . . . . . . . . . . . . . . . . 111−46−6 70. Di−isodecyl phthalate . . . . . . . . . . . . . . . . . . 26761−40−0 71. Dimethyl terephthalate . . . . . . . . . . . . . . . . . 120−61−6 72. 2,4−Dinitrotoluene . . . . . . . . . . . . . . . . . . . . . 121−14−2 73. 2,6−Dinitrotoluene . . . . . . . . . . . . . . . . . . . . . 606−20−2 74. Dioctyl phthalate . . . . . . . . . . . . . . . . . . . . . . 117−81−7

75. Dodecene . . . . . . . . . . . . . . . . . . . . . . . . . . . . 25378−22−7 76. Dodecylbenzene, nonlinear . . . . . . . . . . . . . . 77. Dodecylbenzenesulfonic acid . . . . . . . . . . . . . 27176−87−0 78. Dodecylbenzenesulfonic acid, sodium salt . . . . . . . . . . . . . . . . . . . . . . . . . 25155−30−0

79. Epichlorohydrin . . . . . . . . . . . . . . . . . . . . . . . 106−89−8

80. Ethanol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 64−17−5

81. Ethanolamine . . . . . . . . . . . . . . . . . . . . . . . . . 141−43−5 82. Ethyl acetate . . . . . . . . . . . . . . . . . . . . . . . . . 141−78−6 83. Ethyl acrylate . . . . . . . . . . . . . . . . . . . . . . . . . 140−88−5 84. Ethylbenzene . . . . . . . . . . . . . . . . . . . . . . . . . 100−41−4 85. Ethyl chloride . . . . . . . . . . . . . . . . . . . . . . . . 75−00−3 86. Ethylene dibromide . . . . . . . . . . . . . . . . . . . . 106−93−4 87. Ethylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 74−85−1 88. Ethylene dichloride . . . . . . . . . . . . . . . . . . . . 107−06−2 89. Ethylene glycol . . . . . . . . . . . . . . . . . . . . . . . 107−21−1 90. Ethylene glycol monobutyl ether . . . . . . . . . . 111−76−2 91. Ethylene glycol monoethyl ether acetate . . . . 111−15−9 92. Ethylene glycol monomethyl ether . . . . . . . . 109−86−4 93. Ethylene oxide . . . . . . . . . . . . . . . . . . . . . . . . 75−21−8 94. 2−Ethylhexyl alcohol . . . . . . . . . . . . . . . . . . . 104−76−7 95. (2−Ethylhexyl) amine . . . . . . . . . . . . . . . . . . 104−75−696. 6−Ethyl−1,2,3,4−tetrahydro 9,10−anthracenedione . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 15547−17−8

97. Formaldehyde . . . . . . . . . . . . . . . . . . . . . . . . 50−00−0 98. Glycerol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 56−81−5 99. n−Heptane . . . . . . . . . . . . . . . . . . . . . . . . . . . 142−82−5 100. Heptenes (mixed) . . . . . . . . . . . . . . . . . . . . . . 101. Hexamethylene diamine . . . . . . . . . . . . . . . . 124−09−4 102. Hexamethylene diamine adipate . . . . . . . . . . 3323−53−3 103. Hexamethylenetetramine . . . . . . . . . . . . . . . 100−97−0

104. Hexane . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 110−54−3
105. Isobutane . . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−28−5

106. Isobutanol . . . . . . . . . . . . . . . . . . . . . . . . . . . 78−83−1 107. Isobutylene . . . . . . . . . . . . . . . . . . . . . . . . . . 115−11−7 108. Isobutyraldehyde . . . . . . . . . . . . . . . . . . . . . . 78−84−2 109. Isopentane . . . . . . . . . . . . . . . . . . . . . . . . . . . 78−78−4 110. Isoprene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 78−79−5 111. Isopropanol . . . . . . . . . . . . . . . . . . . . . . . . . . 67−63−0

112. Ketene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 463−51−4 113. Linear alcohols, ethoxylated, mixed . . . . . . . Chemical Name CAS No. 1
114. Linear alcohols, ethoxylated, and sulfated, sodium salt, mixed . . . . . . . . . . . . . . . . . . .
115. Linear alcohols, sulfated, sodium salt, mixed 116. Linear alkylbenzene . . . . . . . . . . . . . . . . . . . . 123−01−3 117. Maleic anhydride . . . . . . . . . . . . . . . . . . . . . . 108−31−6 118. Mesityl oxide . . . . . . . . . . . . . . . . . . . . . . . . . 141−79−7

119. Methanol . . . . . . . . . . . . . . . . . . . . . . . . . . . . 67−56−1 120. Methylamine . . . . . . . . . . . . . . . . . . . . . . . . . 74−39−5 121. ar−Methylbenzenediamine . . . . . . . . . . . . . . . 25376−45−8 122. Methyl chloride . . . . . . . . . . . . . . . . . . . . . . . 74−87−3 123. Methylene chloride . . . . . . . . . . . . . . . . . . . . 75−09−2 124. Methyl ethyl ketone . . . . . . . . . . . . . . . . . . . . 78−93−3 125. Methyl isobutyl ketone . . . . . . . . . . . . . . . . . 108−10−1 126. Methyl methacrylate . . . . . . . . . . . . . . . . . . . . 80−62−6 127. 1−Methyl−2−pyrrolidone . . . . . . . . . . . . . . . 872−50−4 128. Methyl tert−butyl ether . . . . . . . . . . . . . . . . . . 129. Naphthalene . . . . . . . . . . . . . . . . . . . . . . . . . . 91−20−3

130. Nitrobenzene . . . . . . . . . . . . . . . . . . . . . . . . . 98−95−3

131. 1−Nonene . . . . . . . . . . . . . . . . . . . . . . . . . . . 27215−95−8 132. Nonyl alcohol . . . . . . . . . . . . . . . . . . . . . . . . 143−08−8 133. Nonylphenol . . . . . . . . . . . . . . . . . . . . . . . . . . 25154−52−3 134. Nonylphenol, ethoxylated . . . . . . . . . . . . . . . 9016−45−9

135. Octene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 25377−83−7 136. Oil−soluble petroleum sulfonate, calcium salt . 137. Pentaerythritol . . . . . . . . . . . . . . . . . . . . . . . . 115−77−5

138. 3−Pentenenitrile . . . . . . . . . . . . . . . . . . . . . . . 4635−87−4 139. Pentenes, mixed . . . . . . . . . . . . . . . . . . . . . . . 109−67−1 140. Perchloroethylene . . . . . . . . . . . . . . . . . . . . . 127−18−4

141. Phenol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−95−2 142. 1−Phenylethyl hydroperoxide . . . . . . . . . . . . 3071−32−7 143. Phenylpropane . . . . . . . . . . . . . . . . . . . . . . . . 103−65−1 144. Phosgene . . . . . . . . . . . . . . . . . . . . . . . . . . . . 75−44−5 145. Phthalic anhydride . . . . . . . . . . . . . . . . . . . . . 85−44−9 146. Propane . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 74−98−6 147. Propionaldehyde . . . . . . . . . . . . . . . . . . . . . . 123−38−6 148. Propyl alcohol . . . . . . . . . . . . . . . . . . . . . . . . 71−23−8 149. Propylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . 115−07−1 150. Propylene glycol . . . . . . . . . . . . . . . . . . . . . . 57−55−6 151. Propylene oxide . . . . . . . . . . . . . . . . . . . . . . . 75−56−9

152. Sorbitol . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 50−70−4 153. Styrene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 100−42−5 154. Terephthalic acid . . . . . . . . . . . . . . . . . . . . . . 100−21−0 155. Tetraethyl lead . . . . . . . . . . . . . . . . . . . . . . . . 78−00−2 156. Tetrahydrofuran . . . . . . . . . . . . . . . . . . . . . . . 109−99−9 157. Tetra (methyl−ethyl) lead . . . . . . . . . . . . . . . . 158. Tetramethyl lead . . . . . . . . . . . . . . . . . . . . . . 75−74−1

159. Toluene . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−88−3 160. Toluene−2,4−diamine . . . . . . . . . . . . . . . . . . 95−80−7 161. Toluene−2,4−(and, 2,6)−diisocyanate (80/20 mixture) . . . . . . . . . . . . . . . . . . . . . . . . . . . 26471−62−5

162. 1,1,1−Trichloroethane . . . . . . . . . . . . . . . . . . 71−55−6 163. 1,1,2−Trichloroethane . . . . . . . . . . . . . . . . . . 79−00−5 164. Trichloroethylene . . . . . . . . . . . . . . . . . . . . . . 79−01−6

165. Trichlorofluoromethane . . . . . . . . . . . . . . . . . 75−69−4 166. 1,1,2−Trichloro−1,2,2−trifluoroethane . . . . . . 76−13−1

167. Triethanolamine . . . . . . . . . . . . . . . . . . . . . . . 102−71−6 168. Triethylene glycol . . . . . . . . . . . . . . . . . . . . . 112−27−6 169. Vinyl acetate . . . . . . . . . . . . . . . . . . . . . . . . . 108−05−4450−15 NR 440.71 DEPARTMENT OF NATURAL RESOURCES

The Wisconsin Administrative Code on this web site is current through the last published Wisconsin Register . See also Are the Codes on this Website Official? 

### Register, May 2008, No. 629 Chemical Name CAS No. 1 170. Vinyl chloride . . . . . . . . . . . . . . . . . . . . . . . . 75−01−4 171. Vinylidene chloride . . . . . . . . . . . . . . . . . . . . 75−35−4 172. m−Xylene . . . . . . . . . . . . . . . . . . . . . . . . . . . 108−38−3 173. o−Xylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . 95−47−6 174. p−Xylene . . . . . . . . . . . . . . . . . . . . . . . . . . . . 106−42−3 175. Xylenes (mixed) . . . . . . . . . . . . . . . . . . . . . . 1330−20−7

1CAS numbers refer to the Chemical Abstracts Registry numbers assignedto specific chemicals, isomers or mixtures of chemicals. 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 listed whether CAS numbers have been assigned or not.

History: Cr., Register, December, 1995, No. 480 , eff. 1−1−96; CR 06−109 : am. (1) (c) 2., 3. and 4., (5) (d) 2. b. and 4.,(e) 1. a. and (f) 1., (6) (L) 1., 4., 5. and 8. and (8), cr. (1) (d) Register May 2008 No. 629 , eff. 6−1−08; correction in (1) (d) 2. made under s. 13.92 (4) (b) 7. , Stats., Register May 2008 No. 629

. NR 440.71 Magnetic tape coating facilities. (1) APPLICABILITY AND DESIGNATION OF AFFECTED FACILITY. (a)The affected facilities to which the provisions of this section apply are: 1. Each coating operation; and 2. Each piece of coating mix preparation equipment. (b) Any new coating operation that utilizes less than 38 m3 of solvent or any modified or reconstructed coating operation that utilizes less than 370 m3 of solvent for the manufacture of magnetic tape per calendar year is subject only to the requirements of subs. (5) (a)and (8) (b)and (c) . If the amount of solvent utilized for the manufacture of magnetic tape equals or exceeds these amounts in any calendar year, the facility is subject to sub. (3)and all other paragraphs of this section. Once a facility has become subject to sub. (3)and all other paragraphs of this section, it shall remain subject to those requirements regardless of changes in annual solvent utilization. (c) This section applies to any affected facility for which construction, modification or reconstruction begins after January 22, 1986. (2) D EFINITIONS, SYMBOLS AND CROSS REFERENCE TABLES. (a) All terms used in this section that are not defined as follows have the meaning given to them in s. NR 440.02

. 1. “Base film” means the substrate that is coated to produce magnetic tape. 2. “Capture system” means any device or combination of devices that contains or collects an airborne pollutant and directs it into a duct. 3. “Coating applicator” means any apparatus used to apply a coating to a continuous base film. 4. “Coating mix preparation equipment” means all mills, mixers, holding tanks, polishing tanks and other equipment used in the preparation of the magnetic coating formulation but does not include those mills that do not emit VOC because they are closed, sealed and operated under pressure. 5. “Coating operation” means any coating applicator, flashoff area and drying oven located between a base film unwind station and a base film rewind station that coat a continuous base film to produce magnetic tape.6. “Common emission control device” means a control device controlling emissions from the coating operation as well as from another emission source within the plant. 7. “Concurrent” means construction of a control device is commenced or completed within the period beginning 6 months prior to the date construction of affected coating mix preparationequipment commences and ending 2 years after the date construction of affected coating mix preparation equipment is completed. 8. “Control device” means any apparatus that reduces the quantity of a pollutant emitted to the air. 9. “Cover” means, with respect to coating mix preparation equipment, a device that lies over the equipment opening to prevent VOC from escaping and that meets the requirements found in sub. (3) (e) 1. to 5. 10. “Drying oven” means a chamber in which heat is used to bake, cure, polymerize or dry a surface coating. 11. “Equivalent diameter” means 4 times the area of an opening divided by its perimeter. 12. “Flashoff area” means the portion of a coating operation between the coating applicator and the drying oven where solvent begins to evaporate from the coated base film.13. “Magnetic tape” means any flexible substrate that is covered on one or both sides with a coating containing magnetic particles and that is used for audio or video recording or information storage. 14. “Natural draft opening” means any opening in a room, building or total enclosure that remains open during operation of the facility and that is not connected to a duct in which a fan is installed. The rate and direction of the natural draft across suchan opening is a consequence of the difference in pressures on either side of the wall containing the opening. 15. “Nominal 1−month period” means a calendar month or, if established prior to the performance test, a similar monthly time period, for example, 30−day month or accounting month. 16. “Temporary enclosure” means a total enclosure that is constructed for the sole purpose of measuring the fugitive emissions from an affected facility. A temporary enclosure shall be constructed and ventilated, through stacks suitable for testing, so that it has minimal impact on the performance of the permanent capture system. A temporary enclosure will be assumed to achieve total capture of fugitive VOC emissions if it conforms to the requirements found in sub. (4) (b) 5. a. and if all natural draft openings are at least 4 duct or hood equivalent diameters away from each exhaust duct or hood. Alternatively, the owneror operator may apply to the administrator for approval of a temporary enclosure on a case−by−case basis. 17. “Total enclosure” means a structure that is constructed around a s ource of emissions so that all VOC emissions are collected and exhausted through a stack or duct. With a total enclosure, there will be no fugitive emissions, only stack emissions. The only openings in a total enclosure are forced makeup air and exhaust ducts and any natural draft openings such as those that allow raw materials to enter and exit the enclosure for processing. All access doors or windows are closed during routine operation of the enclosed source. Brief, occasional openings of such doors or windows to accommodate process equipment adjustments are acceptable, but, if such openings are routine or ifan access door remains open during the entire operation, the access door shall be considered a naturaldraft opening. The average inward face velocity across the natural draft openings of the enclosure shall be calculated including the area of such access doors. The dr ying oven itself may be part of the total enclosure. A permanent enclosure that meets the requirements found in sub. (4) (b) 5. a.is assumed to be a total enclosure. The owner or operator of a permanent enclosure that does not meet the requirements may apply to the department for approval of the enclosure as a total enclosure on a case−by−case basis. Such approval shall be granted upon a demonstration to the satisfaction of the department that all VOC emissions are contained and vented to the control device. 18. “Utilize” refers to the use of solvent that is delivered to coating mix preparation equipment for the purpose of formulating coatings to be applied on an affected coating operation and any other solvent, for example, dilution solvent, that is added at any point in the manufacturing process.20. “Volatile organic compounds” or ‘VOC‘ means any organic compounds that participate in atmospheric photochemical