3745-21-10 Compliance test methods and procedures.

[Comment: For dates of non-regulatory government publications, publications of recognized organizations and associations, federal rules, and federal statutory provisions referenced in this rule, see the last paragraph of rule 3745-21-01 of the Administrative Code titled"Incorporation by reference."]

(A) General provisions.

(1) The methods and procedures of this rule apply to sources governed by rule 3745-21-09 of the Administrative Code.

(2) Use of an alternative test method, in lieu of one of the USEPA's approved test methods or in lieu of other methods specified in this rule, must be approved by the USEPA as a revision of the state implementation plan.

(3) The results of any compliance testing required by the director for tests conducted pursuant to paragraphs (C) to (F) and (L) of this rule shall not be accepted unless the Ohio EPA district office or local air agency has been notified of the intent to test in accordance with paragraph (A)(4) of this rule not less than thirty days before the proposed initiation of the testing.

(4) Any person notifying the Ohio EPA district office or local air agency of a proposed emissions compliance test shall include as part of the notification the following information:

(a) A statement indicating the purpose of the proposed test and the applicable paragraph of rule 3745-21-09 of the Administrative Code;

(b) A detailed description of the facility to be tested;

(c) A detailed description of the test procedures, equipment and sampling sites; and

(d) A timetable, setting forth the dates on which:

(i) The testing will be conducted; and

(ii) The final test report will be submitted (not later than thirty days after completion of on-site sampling).

(5) For any source compliance determination, the owner or operator of the source shall be responsible for providing:

(a) Sampling ports, pipes, lines, or appurtenances for the collection of samples and data required by the test procedures;

(b) Safe access to the sample and data collection locations; and

(c) Light, electricity, and other utilities required for sample and data collection.

(B) Method for the determination of volatile organic compound content, solids content, and density of surface coatings and inks.

(1) This method applies to coatings, inks or other coating materials employed in a coating line, printing line or other operation. For purposes of this method "coating" shall also mean "ink" or other coating material.

(2) Any determination of VOC content, solids content, or density of a coating shall be based on the coating as employed (as applied), including the addition of any thinner or viscosity reducer to the coating.

(3) When a sample of a coating is obtained for analysis by any of the procedures described in this method, the amount of the sample shall be at least one quart. The sample shall be placed in an air-tight container. When multiple package coatings are sampled, separate samples of each component shall be obtained.

(4) Using either the procedures set forth in USEPA Method 24 (for coatings) and USEPA Method 24A (for flexographic and rotogravure printing inks and related coatings), or the coating formulation data from the coating manufacturer and coating user, the following shall be determined, where appropriate:

Dc = density of coating, in pounds of coating per gallon of coating.

Dvm = density of volatile matter in coating, in pounds of volatile matter per gallon of volatile matter.

Vs = volume fraction of solids (nonvolatile matter) in coating, in gallon of solids per gallon of coating.

Vvm = volume fraction of volatile matter in coating, in gallon of volatile matter per gallon of coating.

Vw = volume fraction of water in coating, in gallon of water per gallon of coating.

Ws = weight fraction of solids (nonvolatile matter) in coating, in pound of solids per pound of coating.

Wvm = weight fraction of volatile matter in coating, in pound of volatile matter per pound of coating. If this weight fraction is determined by ASTM D2369-04, "Standard Test Method for Volatile Content of Coatings," the drying conditions shall be one hundred ten degrees Celsius for one hour, except where otherwise authorized by the director based on an alternate analytical procedure that is satisfactorily demonstrated to the director by the coating manufacturer to be more representative of the actual cure mechanism of the coating.

Ww = weight fraction of water in coating, in pound of water per pound of coating.

(5) If the coating contains a volatile matter other than VOC or water, the identity and content of such volatile matter may be determined using either standard gas chromatographic techniques or coating formulation data from the coating manufacturer and coating user. The density of such volatile matter may be determined using either the procedures set forth in ASTM D1475-98 or data from reference texts. For purposes of this method, such volatile matter shall be referred to as exempt solvent. The following may be determined, where appropriate:

Des = density of exempt solvent, in pounds of exempt solvent per gallon of exempt solvent.

Ves = volume fraction of exempt solvent in coating, in gallon of exempt solvent per gallon of coating.

Wes = weight fraction of exempt solvent in coating, in pound of exempt solvent per pound of coating.

(6) The weight fraction Wvoc of VOC in a coating and the volume fraction Vvoc of VOC in a coating shall be calculated as follows, where appropriate:

Wvoc = Wvm - Ww - Wes

Vvoc = Vvm - Vw - Ves

(7) The VOC content of a coating can be expressed as follows:

Cvoc,1 = VOC content in pounds of VOC per gallon of coating.

Cvoc,2 = VOC content in pounds of VOC per gallon of coating, excluding water and exempt solvents.

Cvoc,3 = VOC content in pounds of VOC per gallon of solids.

Cvoc,4 = VOC content in pounds of VOC per pound of solids.

Cvoc,5 = VOC content in percentage VOC by volume of the coating, excluding water and exempt solvents.

Cvoc,6 = VOC content in percentage VOC by volume of the volatile matter.

Cvoc,7 = VOC content in percentage VOC by weight of the coating.

(8) The VOC content of a coating shall be calculated as follows, where appropriate:

See Calculations at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_RU_20080815_0819.pdf

(9) The weighted average VOC content of the coatings employed during a specified time period t shall be calculated as follows, where appropriate:

See Calculations at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_RU_20080815_0819.pdf

(10) The density of the VOC content of a coating may be determined using either the procedures set forth in ASTM D1475-98 or data from reference texts. If ASTM D1475-98 is employed, the density shall be the arithmetic average of three determinations.

(11) In the event of a dispute between coating formulation data and data obtained by analytical procedures, the data obtained by analytical procedures shall be employed, except as otherwise provided in paragraph (B)(12) of this rule.

(12) If a VOC content value obtained by analytical procedures is higher than a VOC content value obtained by formulation data due to any VOC that is formed during baking or curing (i.e., cure volatiles), then the VOC content of the portion of the coating not subject to curing or baking shall be based on formulation data and the VOC content of the portion of the coating subject to curing or baking shall be based on analytical procedures. The portion of the coating subject to curing or baking shall be equal to the measured transfer efficiency for the coating applicator and object being coated. The approach described in this paragraph for determining the VOC content of a coating may be used only when the applicable VOC limitation is expressed in terms of pounds of VOC per gallon of deposited solids and the transfer efficiency test method is specified in this rule or rule 3745-21-09 of the Administrative Code. Also, in cases where analytical results and formulation data are combined for a waterborne coating, the interlaboratory precision adjustments specified in the analytical procedures shall not be applied to the analytical results.

(C) Method for the determination of VOC concentration, VOC mass emission rate and VOC control equipment efficiency.

(1) The provisions of this paragraph are generally applicable to the test methods employed to determine the VOC concentration and VOC mass emission rate for a gas stream or exhaust vent and the collection or control efficiency for any control equipment designed, installed, and operated for the purpose of reducing the emission of VOC. For purposes of this paragraph, "vapor collection system" also means capture system and "vapor control system" also means control system or control device.

(2) The concentration of VOC in a gas stream or exhaust vent shall be determined by utilizing the following methods:

(a) USEPA Method 25 or USEPA Method, as appropriate, for sources specified in paragraphs (C) to (L), (P), (R), (S), (U), (W) to (Y), (FF), (GG), (LL) to (NN) [if the control efficiency compliance option in (LL), (MM) or (NN) is chosen] and, (PP), (SS), (VV)(2), (XX)(1), (YY), (ZZ)(1)(a), (AAA)(1), and (BBB) of rule 3745-21-09 of the Administrative Code; or

(b) USEPA Method 18) or USEPA Method 25A, as appropriate, for sources specified in paragraphs (O)(3)(c)(iv), (O)(4)(a)(ii), (CC) to (EE), and (LL) to (NN) [if the ppmv compliance option in (LL), (MM) or (NN) is chosen] of rule 3745-21-09 of the Administrative Code.

(3) The following procedures shall be included in any source testing or determination where applicable:

(a) The source shall be operated at or near maximum operating capacity during any testing and the measurement of the operating rate shall be made in a manner acceptable to the Ohio environmental protection agency.

(b) The VOC content of any coatings employed shall be sampled and analyzed in accordance with paragraph (B) of this rule.

(c) The capture efficiency of any vapor collection system used to transport the VOC emissions from their point of origin to the vapor control system shall be determined in accordance with USEPA Methods 204 to 204F or the alternative capture efficiency testing protocols specified in the USEPA, Office of Air Quality Planning and Standards document entitled "Guidelines for Determining Capture Efficiency."

(d) The control efficiency of any vapor control system used to reduce the emission of VOC shall be based upon an emissions test or a recovery test. For a vapor control system that destroys VOC (e.g., an incineration system), either the streams entering and leaving the vapor control system shall be tested or, if acceptable to the director, the amount of VOC employed shall be measured and the gas stream leaving the vapor control system shall be tested. For a vapor control system that recovers VOC (e.g., a carbon adsorption system), either the gas streams entering and leaving the vapor control system shall be tested or, if acceptable to the director, the amounts of VOC employed and recovered or, employed and emitted, shall be measured or tested.

(e) For the testing of a gas stream vented to a vapor control system, samples shall be taken simultaneously at the inlet and the outlet of the vapor control system.

(f) For the testing of a gas stream, the sampling location(s), volumetric flow rate, molecular weight, carbon dioxide and oxygen contents, excess air, and water vapor content shall be determined in accordance with USEPA Methods 1, 1A, 2, 2A, 2C, 2D, 3 and 4.

(g) For gas streams tested by USEPA Method 25 or 25A, the VOC emission rate shall be based upon the average of three test runs. Each run shall have a minimum duration of one hour and a minimum sample volume of .003 dry standard cubic meter, except that shorter sampling times or smaller volumes, when necessitated by process variables, may be found acceptable.

(h) The control efficiency of the vapor control system shall be the per cent reduction in mass emissions of VOC between the inlet and the outlet of the vapor control system. If this efficiency is based upon an emissions test utilizing USEPA Method 25 or 25A, the mass emissions of VOC as carbon shall be employed in the efficiency determination.

(i) The capture efficiency of the vapor collection system shall be the per cent of total mass emissions of VOC emitted from the source which are vented to the vapor control system. If this efficiency is based upon an emissions test utilizing USEPA Method 25 or 25A, the mass emissions of VOC as carbon shall be employed in the efficiency determination.

(j) The overall control efficiency (in per cent) of any control equipment for VOC emissions shall be the vapor capture efficiency multiplied by the vapor control efficiency and divided by one hundred.

(k) The total mass emission rate of VOC from a source equipped with control equipment shall be the sum of VOC emissions from the vapor control system, VOC emissions not collected by the vapor collection system and VOC emissions from any losses associated with the vapor collection system and vapor control system.

(4) The VOC mass emissions rate for a gas stream tested by USEPA Method 18 shall be calculated as follows:

See Calculation at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_RU_20080815_0819.pdf

(5) The mass emission rate of VOC as carbon for a gas stream tested by USEPA method Method 25 shall be calculated as follows:

See Calculation at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_RU_20080815_0819.pdf

(6) To convert a mass emission rate from kilograms per hour to pounds per hour, multiply the mass emission rate in kilograms per hour by 2.2046.

(7) To convert a mass emission value from VOC as carbon to VOC, divide the mass emission value of VOC as carbon by the weight fraction of carbon in the average molecular weight of the VOC emission. The determination of this weight fraction of carbon may be based on standard analytical techniques or material formulation data.

(D) Method for the determination of VOC emissions from solvent metal cleaning:

(1) This method is applicable to determining VOC emissions from solvent metal cleaning equipment.

(2) The purpose of this method is to quantify, by material balance, the amount of solvent input into a degreaser over a sufficiently long period of time so that an average emission rate can be computed.

(3) The following procedure shall be followed to perform a material balance test:

(a) Clean the degreaser sump before testing.

(b) Record the amount of initial and make-up solvent added to the tank with a flow meter or other means.

(c) Record the type and amount or weight of work load degreased each day.

(d) At the end of the test run, pump out the used solvent and measure the amount with a flow meter or other means. Also, estimate the volume of metal chips and other material remaining in emptied sump, if significant.

(e) Bottle a sample of the used solvent and analyze it to find the per cent that is oil and other contaminants. The oil and solvent proportions can be estimated by weighing samples of used solvent before and after boiling off the solvent. Compute the volume of oils in the used solvent. The volume of solvent displaced by this oil along with the volume of make-up solvent added during operations is equal to the amount of VOC emissions.

(4) The following procedure can be followed to perform a material balance test in lieu of the procedure in paragraph (D)(3) of this rule:

(a) Clean the degreaser sump before testing.

(b) Record the amount of initial and make-up solvent added to the tank as measured with a flow meter or other means.

(c) Record the type and amount or weight of work load degreased over the period of the test.

(d) Record the amount of used solvent pumped out of the tank for disposal as measured with a flow meter or other means.

(e) Bottle a sample of the used solvent and analyze it to find the per cent that is oil and other contaminants.

(f) The VOC emissions from solvent metal cleaning equals the total solvent added to the tank minus the solvent contained in the used solvent being disposed.

(E) Method for the determination of VOC emissions from bulk gasoline terminals.

(1) This method is applicable to determining the VOC emission rates at a bulk gasoline terminal employing a vapor collection system and either a continuous or intermittent vapor control system at a loading rack.

(2) The VOC emission rates shall be determined in accordance with the methods and procedures contained in 40 CFR 60.503(b), (c), (e) and (f) of "Subpart XX - Standards of Performance for Bulk Gasoline Terminals," except that the gasoline throughput during any test shall be not less than ninety per cent of the maximum throughput of the loading rack(s) and not less than eighty thousand gallons.

(3) During any test, all loading racks shall be open for each product line which is controlled by the system under test. Simultaneous use of more than one loading rack shall occur to the extent that such use would normally occur.

(4) Simultaneous use of more than one dispenser on each loading rack shall occur to the extent that such use would normally occur.

(5) Dispensing rates shall be set at the maximum rate at which the equipment is typically operated. Automatic product dispensers are to be used according to normal operating practices.

(6) Applicable operating parameters of the vapor control system shall be monitored to demonstrate that the control unit is operating at design levels. Delivery devices shall be leak free.

(7) For each gasoline tank truck loaded during the test period, all potential sources of leaks shall be checked in accordance with the method specified in paragraph (K) of this rule. The tank identification number, the latest leak check certification date, and the location and highest detector reading for each incident of leakage shall be recorded.

(8) During each test, all potential sources of leaks in the vapor collection and control systems shall be monitored in accordance with the method specified in paragraph (K) of this rule. The location and highest detector reading for each incident of leakage shall be recorded.

(F) Method for the detection of leaks of VOC from petroleum refinery equipment and organic chemical manufacturing equipment.

(1) This method is applicable to the detection of leaks of VOC into the ambient air from petroleum refinery equipment and any chemical manufacturing equipment subject to paragraph (T) or (DD) of rule 3745-21-09 of the Administrative Code.

(2) The detection of leaks shall be determined in accordance with the test procedure set forth in USEPA Method 21.

(3) The calibration gases shall be:

(a) Zero air, which consists of less than ten ppmv of hydrocarbon in air; and

(b) A mixture of air and methane or n-hexane at a concentration of approximately, but less than, ten thousand ppmv of methane or n-hexane.

(4) The leak detection instrument shall be calibrated before use on each day of its use.

(G) Standard method for the determination of the leak tightness of gasoline tank trucks (method G).

(1) This method is applicable to determining the leak tightness of gasoline tank trucks which are equipped with piping, hoses and other devices for the collection or return of gasoline vapors during the transfer of gasoline at a gasoline dispensing facility, bulk gasoline plant or bulk gasoline terminal.

(2) The leak tightness of a gasoline tank truck shall be determined in accordance with the test procedure set forth in USEPA Method 27. For the pressure test, the initial pressure shall be 18.0 inches of water. For the vacuum test, the initial vacuum shall be 6.0 inches of water.

(3) If any gasoline tank truck or compartment of a gasoline tank truck sustains either a pressure decrease greater than 3.0 inches of water over five consecutive minutes for the pressure test or a pressure increase greater than 3.0 inches of water over five consecutive minutes for the vacuum test, the tank truck is not leak tight. If not leak tight, repair the tank truck as necessary and repeat the entire test procedure specified in paragraph (G)(2) of this rule until the gasoline tank truck or compartment passes the test.

(H) (Reserved)

(I) Method for the determination of seal gaps in an external floating roof tank.

(1) This method is applicable to determining the width and area of any gaps between the wall of an external floating roof tank and a seal which is around the circumference of the external floating roof.

(2) The width of any seal gap is the distance between the seal and the tank wall. It is determined by using probes of various widths to accurately measure the actual distance from the seal to the tank wall.

(3) The area of any seal gap is determined by multiplying the width of the seal gap, as determined in paragraph (I)(2) of this rule, by the circumferential length of the gap.

(4) The total seal gap area is the accumulated area of all gaps which are greater than 0.125 inch in width.

(J) Method for the determination of the perchloroethylene content of wastes at a dry cleaning facility which uses perchloroethylene.

(1) The method is applicable to determining the perchloroethylene content in per cent by weight for waste at a dry cleaning facility from any distillation operation which distills perchloroethylene and from any diatomaceous earth filter which filters perchloroethylene.

(2) The perchloroethylene content of the waste in per cent by volume is determined in accordance with the procedure in ASTM D322-97(2002)e1, and is calculated as the diluent content in that procedure.

(3) The density of the waste is determined by weighing a known volume of the waste and is calculated as the net weight of the waste in pounds divided by the volume of the waste in gallons.

(4) The perchloroethylene content of the waste in per cent by weight is calculated as the product of its diluent content and 13.55, divided by its density.

(K) Method for the detection of leaks of gasoline vapors from vapor control systems, vapor collection systems, vapor balance systems, gasoline barges and gasoline tank trucks.

(1) This method is applicable to the detection of leaks of gasoline vapors into the ambient air from:

(a) Vapor control systems, vapor collection systems, and vapor balance systems at barge loading facilities (for gasoline), bulk gasoline terminals, bulk gasoline plants, and gasoline dispensing facilities; and

(b) Gasoline barges and gasoline tank trucks during loading, providing the vapor control system, vapor collection system, or vapor balance system which is connected to the gasoline barge or gasoline tank truck does not create a back pressure greater than eighteen inches of water gauge pressure.

(2) This method describes the procedures to be followed for detecting leaks of gasoline vapors by means of a portable hydrocarbon gas analyzer, which is calibrated to read in per cent of the lower explosive limit as propane.

(3) The following equipment are used:

(a) A liquid manometer, or equivalent device, capable of measuring up to twenty-five inches of water gauge pressure with a precision of plus or minus 0.1 inch of water; and

(b) A portable hydrocarbon gas analyzer which:

(i) Is equipped with a sampling line of sufficient length for easy maneuverability during testing and a sampling probe having an internal diameter of 0.25 inch;

(ii) Is certified as safe for operation in explosive atmospheres;

(iii) Has a minimum range of zero to one hundred per cent of the lower explosive limit as propane; and

(iv) Has a response time for full-scale deflection of less than eight seconds with sampling line and probe attached.

(4) The portable hydrocarbon gas analyzer is calibrated with 2.2 per cent propane by volume in air (or equivalent calibration gas) for one hundred per cent of the lower explosive limit according to the procedures and frequency specified by the manufacturer.

(5) The test procedures for detecting leaks are the following:

(a) Connect the liquid manometer to a pressure tap in the vapor control system, vapor collection system, or vapor balance system as close as possible to the connection with the gasoline barge or gasoline tank truck;

(b) Record the pressure periodically during loading of the gasoline barge or gasoline tank truck;

(c) Check with the portable hydrocarbon gas analyzer all potential leak sources on the gasoline barge or gasoline tank truck during loading and on the vapor control system, vapor collection system, or vapor balance system by:

(i) Maintaining the probe's inlet about one inch from the potential leak source in the path of (parallel to) the vapor flow from a leak;

(ii) Moving the probe slowly around the periphery of the potential leak source to locate the point of highest meter response;

(iii) Blocking as much as possible the wind from the area being monitored; and

(d) Record the location of leakage and the highest detector reading for each incidence of leakage.

(L) Method for the determination of the emission of volatile organic compounds from a dryer at a petroleum dry cleaning facility.

(1) This method is applicable to determining the volatile organic compound emission rate of a dryer containing articles cleaned in petroleum solvent at a dry cleaning facility.

(2) The dryer shall be tested under normal operating conditions for at least thirty dryer loads that total not less than four thousand pounds dry weight of articles cleaned. The dryer loads shall represent a normal range of variations in fabrics, solvents, load weights, temperatures, flow rates, and process deviations. Each dryer load shall be tested in accordance with paragraph (L)(3) or (L)(4) of this rule.

(3) For each dryer load the following shall be conducted and recorded:

(a) Determine the average stack gas dry volumetric flow rate V (in dry standard cubic feet per hour) in accordance with USEPA Methods 1 and 2.

(b) Determine the average organic concentration C in the stack (in ppmv as propane) in accordance with USEPA Method 25A in which the flame ionization analyzer is calibrated with propane standards.

(c) Determine the ratio R of the flame ionization analyzer's response to a given parts per million by volume concentration of propane to its response to the same parts per million by volume concentration of the volatile organic compounds present in the stack gas.

(d) Determine the molecular weight M (in pounds per pound-mole) of the volatile organic compounds present in the stack gas. Such determination shall be based on data from the manufacturer of the cleaning solvent or on standard analytical techniques.

(e) Measure and record the weight Wa (in pounds dry weight) of the articles to be cleaned.

(f) Calculate the weight Wvoc (in pounds) of the volatile organic compounds emitted into the ambient air using the following equation:

Wvoc = V X C X R X M

(4) For each dryer load the following shall be conducted and recorded:

(a) All weights shall be measured to the nearest 0.5 pound or less on a scale that is accurate to 0.5 pound at weights of up to two hundred pounds.

(b) Measure and record the weight Wa (in pounds) of the articles to be cleaned.

(c) Measure and record the initial weight Wi (in pounds) of the articles to be dried after the washing cycle.

(d) Measure and record the final weight Wf (in pounds) of the articles removed from the dryer after the drying cycle.

(e) Measure and record the weight Wr (in pounds) of any recovered liquid materials.

(f) Calculate the weight Wvoc (in pounds) of the volatile organic compounds emitted into the ambient air using the following equation:

Wvoc = Wi - Wf - Wr

(5) The dryer's volatile organic compound emission rate (in pounds per one hundred pounds dry weight of articles cleaned) shall be calculated for the combined dryer loads tested under this method as equal to one hundred multiplied by the sum total of Wvoc and divided by the sum total of Wa.

(M) Method for the determination of the amount of volatile organic compounds contained in filtration waste at a petroleum dry cleaning facility.

(1) This method is applicable to determining the amount of volatile organic compounds contained in the waste from a solvent filter used to filter petroleum solvent at a dry cleaning facility.

(2) The solvent filter shall be tested under normal operating conditions for at least three time periods according to the procedures specified in paragraph (M)(3) of this rule.

(3) The test procedures for each time period are as follows:

(a) A time period consists of the time immediately after the removal of waste from the solvent filter up to the next removal of waste.

(b) Record the date and time of the start of the time period.

(c) Record during the time period the weight of articles being cleaned in any washer connected to the solvent filter.

(d) Record the weight of the waste from the solvent filter at the end of the time period, in pounds.

(e) Collect in a sealed container, which is impervious to petroleum solvent, about two pounds of the waste from the solvent filter at the end of the time period.

(f) Record the date and time of the end of the time period.

(g) Conduct a laboratory analysis of the waste collected in the sealed container according to the procedures specified in paragraph (M)(4) of this rule.

(4) The procedures for the laboratory analysis of the collected filtration waste are as follows:

(a) Determine the weight Ws (in grams of a sample of approximately fifty milliliters of the filtration waste).

(b) Determine the volume Vs (in milliliters) of the diluent content of that sample in accordance with ASTM D322-97(2002)e1.

(c) Calculate the sample's diluent content Ds (fraction diluent by weight) using the following equation:

See Equation at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_RU_20080815_0819.pdf

(5) For the test conducted under paragraphs (M)(2), (M)(3) and (M)(4) of this rule, the amount of VOCs contained in the filtration waste is calculated using the following equation:

See Equation at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_RU_20080815_0819.pdf

(N) Method for the determination of the length of time to operate the recovery cycle of a solvent recovery dryer at a petroleum dry cleaning facility.

(1) This method is applicable to determining the length of time for operating the solvent recovery cycle of a solvent recovery dryer at a petroleum dry cleaning facility in order to assure that the flow rate of recovered petroleum solvent at the termination of solvent recovery cycle is no greater than fifty milliliters per minute.

(2) The dryer shall be tested under normal operating conditions for a duration of no less than two weeks during which no less than one-half of the dryer loads shall be monitored for their final recovered solvent flow rate.

(3) The suggested point for measuring the flow rate of recovered solvent is from the outlet of the solvent-water separator. Near the end of the recovery cycle, the entire flow of recovered solvent is diverted to a graduated cylinder. As the recovered solvent collects in the graduated cylinder, the elapsed time is monitored and recorded in periods greater than or equal to one minute. At the same time, the volume of solvent in the graduated cylinder is monitored and recorded to determine the volume of recovered solvent that is collected during each time period. The recovered solvent flow rate is calculated by dividing the volume of solvent collected per period by the length of time elapsed during the period and converting the result with appropriate factors into units of milliliters per minute. The recovery cycle and the monitoring procedure is continued until the flow rate of solvent is less than or equal to fifty milliliters per minute. The date, the type of articles cleaned, and the total length of the recovery cycle shall be recorded for each dryer load being monitored.

(O) Method for the determination of equipment in VOC service and in light liquid service.

(1) This method is applicable to equipment at a petroleum refinery or a process unit subject to paragraph (T) or (DD) of rule 3745-21-09 of the Administrative Code.

(2) Any piece of equipment is presumed to be in VOC service, unless the owner or operator demonstrates that the piece of equipment is not in VOC service according to the following provisions:

(a) The piece of equipment is considered not in VOC service if it can be determined that the VOC content of the process fluid, which is contained in or contacts the piece of equipment, can be reasonably expected never to exceed ten per cent by weight.

(b) For purposes of determining the VOC content of a process fluid, procedures that conform to the general methods described in ASTM E168-99(2004), ASTM E169-04, and ASTM E 260-73 shall be used.

(c) The owner or operator may use engineering judgment rather than the procedures contained in paragraph (O)(2)(b) of this rule to demonstrate that the VOC content of a process fluid does not exceed ten per cent by weight, provided the VOC content clearly does not exceed ten per cent by weight. In the event the Ohio EPA or the USEPA has a disagreement with an engineering judgment, paragraph (O)(2)(b) of this rule shall be used to resolve the disagreement.

(3) A piece of equipment is in light liquid service if it contains or is in contact with a process fluid that meets all of the following conditions:

(a) The process fluid is a liquid at operating conditions.

(b) The vapor pressure of one or more of the pure components within the process fluid is greater than 0.04 pound per square inch at sixty-eight degrees Fahrenheit. Vapor pressures may be obtained from standard reference texts or may be determined by the method in ASTM D 2879-70.

(c) The total concentration of the pure components having a vapor pressure greater than 0.04 pound per square inch at sixty-eight degrees Fahrenheit is equal to or greater than twenty per cent by weight.

(P) Method for the determination of the net heating value of a gas, the actual exit velocity for a flare, and the maximum permitted velocity for an air-assisted flare.

(1) This method is applicable to:

(a) Any flare subject to paragraph (DD) of rule 3745-21-09 of the Administrative Code; and

(b) Any process vent stream subject to paragraph (EE) of rule 3745-21-09 of the Administrative Code.

(2) The net heating value of gas being combusted in a flare or being vented from a process vent stream shall be calculated using the following equation:

See Equation at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_RU_20080815_0819.pdf

(3) The actual exit velocity of a flare shall be calculated by dividing the volumetric flow rate (in units of standard temperature and pressure) of the flare header or headers that feed the flare, as determined by USEPA Methods 2, 2A, 2C, or 2D as appropriate, by the unobstructed (free) cross-sectional area of the flare tip, as determined by design and engineering principles.

(4) The maximum permitted velocity of an air-assisted flare shall be determined by the following equation:

See Equation at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_RU_20080815_0819.pdf

(5) To express the net heating value of a gas in Btu per standard cubic foot, multiply Ht by 26.84.

(6) To express a velocity in feet per second, multiply the velocity in meters per second by 3.281.

(Q) Method for the detection of leaks of gasoline vapors from a vapor control system installed at a gasoline dispensing facility (static leak test).

(1) This method is applicable to quantifying the vapor tightness of a vapor balance system or a vacuum assist control system installed at a gasoline facility.

(2) This method describes the procedures to be followed for detecting leaks of gasoline vapors by pressurizing the entire vapor recovery control system to two inches of water column and then allowing the system pressure to decay for five minutes. The acceptability of the final pressure is based upon the vapor system volume or ullage space. The allowable five minute final pressure is based upon the gasoline tank ullage, pressure decay equations, and the number of affected nozzles.

(3) The equipment, procedures, and pressure decay leak criteria are specified in appendix A of this rule.

(R) Method for the determination of the dynamic pressure performance for a vapor control system installed at a gasoline dispensing facility (dynamic pressure performance test).

(1) This method is applicable to determining the dynamic pressure at known dispensing flow rates for a vapor control system installed at a gasoline dispensing facility. This method is used to quantify the back pressure and detect liquid obstructions in the vapor path leading from the dispensing nozzle to the gasoline storage tank.

(2) This method describes the procedures to be followed in simulating the dynamic back pressures associated with known gasoline dispensing rates and liquid blockages by passing nitrogen through the vapor control system at three flow rates after liquid gasoline has been introduced into the vapor return piping.

(3) The equipment, procedures, and dynamic pressure performance criteria are identified in appendix B of this rule.

APPENDIX A

STATIC LEAK TEST

(taken from BAAQMD test procedure ST-30)

1. Applicability

1.1 This test procedure is used to quantify the vapor tightness of vapor control systems installed at any gasoline dispensing facility (GDF) equipped with pressure/vacuum (P/V) valves, provided that the designed pressure setting of the P/V valves is a minimum of 2.5 inches of water column (inches H2O). Excessive leaks in the vapor control system will increase the quantity of fugitive hydrocarbon emissions and lower the overall efficiencies of both the Stage I and Stage II vapor control systems.

1.2 For those systems equipped with a P/V valve(s) allowed to have a designed cracking pressure less than 2.5 inches H2O, the valve(s) shall be bagged to eliminate, from the test results, any flow contribution through the valve assembly. The valve/vent pipe connection, however, shall remain unobstructed during this test.

1.3 For those facilities not required to be equipped with a P/V valve(s), the vent pipe(s) shall be capped. For these installations, the test may be conducted at the vent pipe(s).

2. Principle

2.1 The entire vapor control system is pressurized with nitrogen to two ( 2.0 ) inches H2O. The system pressure is then allowed to decay and the pressure after five (5) minutes is compared with an allowable value. The minimum allowable five-minute final pressure is based on the system ullage and pressure decay equations. For the purpose of compliance determination, this test shall be conducted after all back-filling, paving, and installation of all Stage I and Stage II components, including P/V valves, has been completed.

2.2 For a GDF equipped with a coaxial Stage I system this test shall be conducted at a Stage II vapor riser. For a GDF which utilizes a two-point Stage I system this test shall be conducted at the Stage I vapor coupler, provided that the criteria set forth in Section 6.7 have been met. If the integrity criteria for two-point systems specified in Section 6.7 are met, this test shall be conducted at the Stage I vapor coupler unless the vapor control system possesses a design which is incompatible with testing at this location.

3. Range

3.1 If mechanical pressure gauges are employed, the full-scale range of the pressure gauges shall be 0- 2.0, 0- 1.0, and 0- 0.50 inches H2O column. Maximum incremental graduations of the pressure gauge shall be 0.05 inches H2O and the minimum accuracy of the gauge shall be three percent of full scale. The minimum diameter of the pressure gauge face shall be 4 inches.

3.2 If an electronic pressure measuring device is used, the full-scale range of the device shall not exceed 0-10 inches H2O with a minimum accuracy of 0.5 percent of full-scale. A 0-20 inches H2O device may be used, provided the equivalent accuracy is not less than 0.25 percent of full scale.

3.3 The minimum ullage during the test shall be 25 percent of the tank capacity (total of alltanks if manifolded) or 500 gallons, whichever is greater. The maximum total ullage shall be 25,000 gallons. These values are exclusive of all vapor piping volumes.

3.4 The minimum and maximum nitrogen feed-rates, into the system, shall be one (1) and five (5) CFM, respectively.

4. Interferences

4.1 Nitrogen shall not be introduced into the system at flowrates exceeding five (5) CFM as this may bias the results of the test toward non-compliance.

4.2 For vacuum-assist Stage II systems which utilize an incinerator, power to the collection unit shall be turned off during testing.

4.3 For vacuum-assist systems which locate the vacuum producing device in-line, between the Stage II vapor riser and the storage tank, the following shall apply:

4.3.1 A valve shall be installed at the vacuum producing device. When closed, this valve shall isolate the vapor passage downstream of the vacuum producing device.

4.3.2 The storage tank side of the vacuum producing device shall be tested in accordance with the procedures outlined in Section 7 of this method. Compliance shall be determined by comparing the final five-minute pressure with the allowable minimum five-minute final pressure from the first column (1-6 affected nozzles) in Table IB or use the corresponding equation in Section 9.2.

4.3.3 The upstream vapor passage (nozzle to vacuum producing device) shall also be tested. Methodology for this test shall be submitted to the Ohio EPA, Division of Air Pollution Control for approval prior to submission of test results or shall be conducted in accordance with the procedures set forth in the applicable CARB certification.

5. Apparatus

5.1 Nitrogen. Use commercial grade nitrogen in a high pressure cylinder, equipped with a two-stage pressure regulator and a one psig pressure relief valve. A one psig (maximum) pressure relief valve is required and mustbe present. In addition, the cylinder of nitrogen mustbe grounded.

5.2 Pressure Measuring Device. Use 0- 2.0, 0- 1.0, and 0- 0.50 inches H2O pressure gauges connected in parallel, a 0-2 inches H2O manometer, or an electronic pressure measuring device to monitor the pressure decay in the vapor control system. The pressure measuring device shall, at a minimum, be readable to the 0.05 inches H2O.

5.3 "T" Connector Assembly. See Figure 1 below for example.

Figure 1

"T" Connector Assembly

See Figure at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP1_20080815_0819.pdf

5.4 Vapor Coupler Integrity Assembly. Assemble OPW 633-A, 633-B, and 634-A adapters, or equivalent, as shown in Figure 2 below. If the test is to be conducted at the storage tank Stage I vapor coupler, this assembly shall be used prior to conducting the static leak test in order to verify the pressure integrity of the vapor poppet. The internal volume of this assembly shall not exceed 0.1 cubic feet.

Figure 2

Vapor Coupler Integrity Assembly

See Figure at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP1_20080815_0819.pdf

5.5 Vapor Coupler Test Assembly. Use a compatible OPW 634-B cap, or equivalent, equipped with a center probe to open the poppet, the appropriate pressure measuring device to monitor the pressure decay, and a connection for the introduction of nitrogen into the system. See Figure 3 below for example.

Figure 3

Vapor Coupler Test Assembly

See Figure at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP1_20080815_0819.pdf

5.6 Stopwatch. Use a stopwatch accurate to within 0.2 seconds.

5.7 Flowmeter. Use a Dwyer flowmeter, Model RMC-104, or equivalent, to determine the required pressure setting of the delivery pressure gauge on the nitrogen supply pressure regulator. This pressure shall be set such that the nitrogen flowrate is between 1.0 and 5.0 CFM.

5.8 Combustible Gas Detector. A Bacharach Instrument Company, Model 0023-7356, or equivalent, may be used to verify the pressure integrity of system components during this test.

5.9 Leak Detection Solution. Any liquid solution designed to detect vapor leaks may be used to verify the pressure integrity of system components during this test.

6. Pre-Test Procedures

6.1 The following safety precautions shall be followed:

6.1.1 Only grounded nitrogen shall be used to pressurize the system.

6.1.2 A one psig relief valve shall be installed to prevent the possible over-pressurizing of the storage tank.

6.2 Product dispensing shall not occur during the test. There shall have been no Stage I deliveries into or out of the storage tanks within the three hours prior to the test. For vacuum-assist Stage II systems, product dispensing shall not occur during the thirty minutes immediately prior to the test.

6.3 Measure the gallons of gasoline present in each underground storage tank and determine the actual capacity of each storage tank from facility records. Calculate the ullage space for each tank by subtracting the gasoline gallonage present from the actual tank capacity. The minimum ullage during the test shall be 25 percent of the tank capacity (total of alltanks if manifolded) or 500 gallons, whichever is greater. The total ullage shall not exceed 25,000 gallons.

6.4 For two-point Stage I systems, this test shall be conducted with the dust cap removed from the vapor coupler. This is necessary to determine the vapor tightness of the Stage I vapor poppet. See Section 6.7 if this test is to be conducted at the Stage I vapor coupler.

6.4.1 For coaxial Stage I systems this test shall be conducted with the dust cap removed from the Stage I coupler. This is necessary to insure the vapor tightness of the Stage I vapor poppet.

6.4.2 Verify that the liquid level in the storage tank is at least four (4) inches above the highest opening at the bottom of the submerged drop tube.

6.5 If the Stage I containment box is equipped with a drain valve, the valve assembly may be cleaned and lubricated prior to the test. This test shall, however, be conducted with the drain valve installed and the manhole cover removed. See subsection 7.4.1 for further details regarding containment box drain valves.

6.6 If the test is to be conducted at a Stage II vapor riser, disconnect the dispenser end of one vapor control hose and install the "T" connector assembly (see Figure 1). Connect the nitrogen gas supply (do not use air) and the pressure measuring device to the "T" connector.

6.6.1 For those Stage II systems utilizing a dispenser mounted remote vapor check valve, the "T" connector assembly shall be installed on the vapor riser side of the check valve.

6.7 If this test is to be conducted at the Stage I vapor coupler on a two-point Stage I system, the procedures set forth in subsections 6.7.1 and 6.7.2 shall be successfully completed prior to testing. The static leak test shall not be conducted at the Stage I coupler at facilities equipped with coaxial Stage I systems.

6.7.1 Connect the Vapor Coupler Integrity Assembly to the Stage I vapor coupler. Connect the Vapor Coupler Test Assembly. Connect the nitrogen supply to the assembly and carefully pressurize the internal volume of the assembly to two ( 2.0 ) inches H2O. Start the stopwatch. Record the final pressure after one minute.

6.7.2 If the pressure after one minute is less than 0.25 inches H2O, the leak rate through the Stage I vapor poppet precludes conducting the static leak test at this location. Repair or replace the faulty component(s) as necessary and restart the test pursuant to Section 6.7.1. If the pressure after one minute is greater than or equal to 0.25 inches H2O, the static leak test may be conducted at this location. This criteria assures a maximum leak rate through the Stage I vapor poppet of less than 0.0004 cubic feet per minute.

6.7.3 Disconnect the Vapor Coupler Integrity Assembly from the Stage I vapor coupler. If the requirements of subsection 6.7.2 were met, install the Vapor Coupler Test Assembly to the Stage I vapor coupler.

6.8 All pressure measuring device(s) shall be bench calibrated using either a reference gauge or incline manometer. Calibration shall be performed at 20, 50, and 80 percent of full scale. Accuracy shall be within two percent at each of these calibration points. Calibrations shall be conducted on a frequency not to exceed 90 days. The individual conducting the test shall supply to the Ohio EPA or its designated local air agency with proof of equipment calibration meeting the requirements of this Section.

6.9 Use the flowmeter to determine the nitrogen regulator delivery pressures which correspond to nitrogen flowrates of 1.0 and 5.0 CFM. These pressures define the allowable range of delivery pressures acceptable for this test procedure. Also record which regulator delivery pressure setting, and the corresponding nitrogen flowrate, will be used during the test.

6.10 Use Equation 9.3 to calculate the approximate time required to pressurize the system ullage to the initial starting pressure of two ( 2.0 ) inches H2O. This will allow the tester to minimize the quantity of nitrogen introduced into those systems which cannot comply with the static leak standards.

6.11 Attach the Vapor Coupler Test assembly to the Stage I poppet or the "T" connector assembly to the Stage II vapor riser. Read the initial pressure of the storage tank and underground piping. If the initial pressure is greater than 0.5 inches H2O, carefully bleed off the pressure, in accordance with all applicable safety procedures, in the storage tank and underground piping to less than 0.5 inches H2O column.

7. Testing

7.1 Open the nitrogen gas supply valve and set the regulator delivery pressure within the allowable range determined in Section 6.9, and start the stopwatch. Pressurize the vapor system (or subsystem for individual vapor return line systems) to at least2.2 inches H2O initial pressure. It is critical to maintain the nitrogen flow until the pressure stabilizes, indicating temperature and vapor pressure stabilization in the tanks. Check the test equipment using leak detecting solution or a combustible gas detector to verify that all test equipment is leak tight.

7.1.1 If the time required to achieve the initial pressure of two ( 2.0 ) inches H2O exceeds twice the time derived from Equation 9.3, stop the test and use liquid leak detector, or a combustible gas detector, to find the leak(s) in the system. Repair or replace the faulty component(s) and restart the test pursuant to Section 7.1.

7.2 Close and disconnect the nitrogen supply. Start the stopwatch when the pressure has decreased to the initial starting pressure of two ( 2.0 ) inches H2O.

7.3 At one-minute intervals during the test, record the system pressure. After five minutes, record the final system pressure. See the applicable of Table IA (or Equation 9.1 ) or IB (or Equation 9.2 ) to determine the acceptability of the final system static pressure results. For intermediate values of ullage in Table IA and IB, linear interpolation may be employed.

7.4 If the system failed to meet the criteria set forth in Table I (or the appropriate equation in Section 9), repressurize the system and check all accessible vapor connections using leak detector solution or a combustible gas detector. If vapor leaks in the system are encountered, repair or replace the defective component and repeat the test. Potential sources of leaks include nozzle check valves, pressure/vacuum reliefvalves, containment box drain valve assemblies, and plumbing connections at the risers.

7.4.1 If the facility fails to comply with the static leak test standards and the Stage I system utilizes a non-CARB-certified drain valve equipped containment box, which was installed prior to July 1, 1992, for which a CARB-certified replacement drain valve assembly is not marketed, the following two subsections shall apply:

7.4. 1.1 The drain valve may be removed and the port plugged. Retest the system. If the facility complies with the static leak test standards under these conditions, the facility shall be considered complying with the requirements, provided that the manufacturer and model number of the containment box and the date of installation are submitted with the test results.

7.4. 1.2 The criteria set forth in subsection 7.4. 1.1 shall not apply after July 1, 1996.

7.5 After the remaining system pressure has been relieved, remove the Vapor Coupler Test Assembly or "T" connector assembly and reconnect the vapor control hose, if applicable.

7.6 If the vapor control system utilizes individual vapor return lines, repeat the leak test for each gasoline grade. Avoid leaving any vapor return line open longer than is necessary to install or remove the "T" connector assembly.

8. Post-Test Procedures

8.1 Use the applicable of Table IA or IB, or the applicable of Equations 9.1 or 9.2, to determine the compliance status of the facility by comparing the final five-minute pressure with the minimum allowable final pressure.

8.1.1 For balance Stage II systems use Table IA or the applicable of Equation 9.1 to determine compliance.

8.1.2 For vacuum-assist Stage II systems use Table IB or the applicable of Equation 9.2 to determine compliance.

9. Calculations

9.1 For Stage II Balance Systems, the minimum allowable five-minute final pressure, with an initial pressure of two ( 2.0 ) inches H2O, shall be calculated as follows:

[Equation 9-1]

See Equation at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP1_20080815_0819.pdf

9.2 For Stage II Vacuum Assist Systems, the minimum allowable five-minute final pressure, with an initial pressure of two ( 2.0 ) inches H2O, shall be calculated as follows:

[Equation 9-2]

See Equation at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP1_20080815_0819.pdf

9.3 The minimum time required to pressure the system ullage to two ( 2.0 ) inches H2O shall be calculated as follows:

[Equation 9-3]

See Equation at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP1_20080815_0819.pdf

9.4 If the policy of the local district requires an allowable tolerance for testing error, the minimum allowable five-minute final pressure, including testing error, shall be calculated as follows:

[Equation 9-4]

See Equation at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP1_20080815_0819.pdf

10. Reporting

10.1 The calculated ullage and system pressures for each five-minute vapor control system test shall be reported as shown in Form 1. Be sure to include the Stage I system type (two-point or coaxial), the Stage II system type, whether the system is manifolded, and the one-minute pressures during the test. The tester may either provide all information listed in Form 1 in the comprehensive test report or include a copy of this form along with the comprehensive written report.

Form 1

Source Test Results

Static Leak Test

See Form at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP1_20080815_0819.pdf

TABLE IA

STAGE II BALANCESYSTEMS

PRESSURE DECAY LEAK RATE CRITERIA

See Table at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP1_20080815_0819.pdf

TABLE IB

STAGE II ASSISTSYSTEMS

PRESSURE DECAY LEAK RATE CRITERIA

See Table at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP1_20080815_0819.pdf

APPENDIX B

DYNAMIC PRESSURE PERFORMANCE TEST

(taken from BAAQMD test procedure ST-27)

1. APPLICABILITY

1.1 This procedure is used to verify compliance with the applicable dynamic back pressure limits imposed on any Stage II vapor control system. The applicability of the following Alternate Methods is dependent upon the regulatory requirements imposed by the CARB certification.

1.1.1 Alternate Method 1.This procedure is applicable if the dynamic back pressure standards are imposed from the nozzle to the gasoline storage tank, provided remote vapor check valves are not part of the Stage II system.

1.1.2 Alternate Method 2.This procedure is applicable if the dynamic back pressure standards are imposed from the Stage II riser to the gasoline storage tank, provided there is no vacuum-producing device located between the riser and tank.

1.1.3 Alternate Method 3.This procedure is applicable if the dynamic back pressure standards are imposed at the nozzle/vehicle interface during vehicle fueling.

1.1.4 Alternate Method 4.This procedure shall be conducted, in conjunction with the applicable of Alternate Methods 1, 2, or 3 if the Stage II system utilizes an incinerator.

1.2 Alternate Methods 1 and 2 shall be conducted with the Stage I vapor poppet open.Alternate Methods 3 and 4 shall be conducted with the poppet closed.

1.3 Other Alternate Methods may be used provided that written approval has been granted by the Ohio EPA, Division of Air Pollution Control. Such approval shall be based upon demonstrated equivalency of any proposed methodology.

2. Principle

2.1 Using Alternate Methods 1, 2, or 4, the dynamic back pressure during vehicle fueling is simulated by passing nitrogen through the Stage II vapor control system at specified rates. The resultant dynamic back pressure is measured using a pressure gauge, or equivalent device. Alternate Method 3 is a direct measurement of the pressure at the nozzle/fillpipe interface during gasoline dispensing. Liquidblockages in the vapor return lines are also detected using these Methods.

3. Range

3.1 The minimum and maximum dynamic back pressures that can be measured are dependent upon the range of the pressure gauges used. Required gauge ranges are as follows:

3.1.1 Alternate Method 1. 0- 0.5 and 0-2 inches H20.

3.1.2 Alternate Method 2. 0- 0.25, 0-1, and 0-2 inches H2O.

3.1.3 Alternate Method 3. - 1.0 -+ 1.0 inches H2O.

3.1.4 Alternate Method 4. 0- 0.5 and 0-1 inches H2O.

3.2 If mechanical pressure gauges are employed, the minimum diameter of the gauge face shall be four inches, and the minimum accuracy of the gauge shall be three percent of full scale.

3.3 If an electronic pressure measuring device is used, the full-scale range of the device shall not shall not exceed 0-10 inches H2O with a minimum accuracy of 0.5 percent of full scale. A 0-20 inches H2O device may be used provided that the equivalent accuracy is not less than 0.25 percent of full-scale.

4. Interferences

4.1 Any leaks in the nozzle vapor path, vapor hose, or underground vapor return piping may result in erroneously low dynamic back pressure measurements.

4.2 For those Stage II systems possessing a design incompatible with this test procedure, testing shall be conducted in accordance with the procedures specified in the applicable CARB Executive Order.

5. Apparatus

5.1 Nitrogen High Pressure Cylinder with Pressure Regulator. Use a high pressure nitrogen cylinder capable of maintaining a pressure of 2000 psig and equipped with a compatible two-stage pressure regulator and a one psig relief valve. The nitrogen cylinder mustbe grounded and the one psig (maximum) relief valve mustbe present during the test.

5.2 Rotameter. Use a calibrated rotameter capable of accurately measuring nitrogen flowrate(s) applicable for the imposed dynamic back pressure limits.

5.3 Pressure Gauges. Use differential pressure gauges, or equivalent, as specified in the applicable subsection of Section 3.1.

5.4 Automobile fillpipe. Use an automobile fillpipe, if applicable, known to be compatible with all bellows-equipped vapor control nozzles, and equipped with a pressure tap. See Figure 1.

5.5 Nitrogen. Use commercial grade nitrogen.

5.6 Hand Pump. Use a gasoline compatible hand pump, if applicable, to drain any gasoline from condensate pots.

5.7 Stopwatch. For Alternate Method 3, use a stopwatch, or equivalent, accurate to within 0.5 seconds.

6. Pre-test procedures

6.1 Alternate Method 1.The following subsections are applicable for those Stage II systems where a limitation is imposed on the dynamic back pressure between the nozzle and the gasoline storage tank, provided that remote vapor check valves are not employed. For those Stage II systems which do notutilize a remote vapor check valve, assemble the apparatus as shown in Figure 1, ensuring that the riser shut-off valve on the test equipment is closed. If a Hirt Stage II system is used, the vacuum producing device shall be turned off during this test.

6.1.1 Assemble the Dynamic Pressure Performance Test Assembly as shown in Figure 1.

6.1.2 The test equipment mustbe leak-checked prior to use. Plug the nozzle end of the auto fillpipe and open the nitrogen cylinder. Adjust the flow meter control valve until a pressure of 50 percent of full scale is indicated on the high range pressure gauge. Close the nitrogen cylinder valve and any toggle valves. A pressure decay of less than 0.2 inches H2O, in five minutes, is considered acceptable.

6.1.3 Perform an initial visual examination for vapor leaks at the nozzles and hoses of the Stage II system to be tested. All leak sources shall be repaired or the component(s) removed and replaced prior to testing.

6.1.4 The Stage I vapor poppet shall be propped open in such a manner that the valve is not damaged. This may be accomplished using a Dynamic Pressure Release Assembly as shown in Figure 2.

6.1.5 Pour a minimum of two (2) gallons of gasoline into each and every Stage II vapor return riser. This gasoline may be introduced into the Stage II riser in any appropriate manner. Alternatively, a minimum of twenty gallons of gasoline may be introduced into the Stage II riser furthest from the gasoline storage tank, provided that the riser is common to all products available at that dispenser. If product-specific risers are employed, a minimum of seven gallons, per product grade, may be introduced into the riser of each product which is furthest from the gasoline storage tank.

6.1.6 Allow fifteen (15) minutes for liquid in the vapor return piping to drain.

6.1.7 Completely drain any gasoline from the spout and bellows of each nozzle.

6.1.8 For those vapor piping configurations which utilize a condensate pot, drain the pot prior to testing.

6.2 Alternate Method 2.

6.2.1 Assemble the Capped "T" Assembly as shown in Figure 3.

6.2.2 Open the Stage I vapor poppet for the affected tank(s).

6.2.3 Pour a minimum of two (2) gallons of gasoline into each and every Stage II vapor return riser. This gasoline may be introduced into the Stage II riser(s) in any appropriate manner.

6.2.4 Allow fifteen (15) minutes for liquid in the vapor return piping to drain.

6.2.5 For those vapor piping configurations which utilize a condensate pot, drain the pot prior to testing.

6.3 Alternate Method 3.

6.3.1 Assemble the Torus Pressure Test Assembly as shown in Figure 4.

6.3.2 The Stage I vapor poppet shall remain closed during this test.

6.4 Alternate Method 4.

6.4.1 Assemble the Vent Pipe Pressure Assembly as shown in Figure 5.

6.4.2 Carefully remove the vent pipe pressure/vacuum (P/V) valve.

6.4.3 Open the Stage I vapor poppet for the affected tank(s).

6.4.4 Insure that the collection unit of the Stage II system is turned off.

7. TESTING

7.1 Alternate Method 1.Insert the nozzle into the fillpipe of the Dynamic Pressure Performance Test Unit as shown in Figure 1 below, ensuring that a tight seal at the fillpipe/nozzle interface is achieved.

7.1.1 Connect the nitrogen supply to the test assembly.

7.1.2 Open the nitrogen supply, set the delivery pressure to 5 psig, and use the flowmeter control valve to adjust the flowrate to lowest of the required nitrogen flowrates.

7.1.3 A pulsating gauge needle indicates nitrogen passing through a liquid obstruction in the vapor return system. Close the flow meter control valve, redrain the nozzle and hose assembly, and repeat the test. If this condition re-occurs, the cause of the liquid trap in the system must be corrected.

Figure 1

Dynamic Pressure Performance Test Assembly

See Figure at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP2_20080815_0819.pdf

7.1.4 The following information shall be recorded on the field data sheet, as shown in Form 1:

(a) Nozzle Number

(b) Gauge needle action

(c) Dynamic back pressure, inches H2O

Specified nitrogen flowrates and associated maximum allowable Dynamic Backpressures are included in Form 1.

7.1.5 Repeat subsections 7.1.2 through 7.1.4 at all required nitrogen flowrates for each and every nozzle.

7.1.6 Close and replace the dust cover on the Stage I poppet.

Figure 2

Dynamic Pressure Release Assembly

See Figure at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP2_20080815_0819.pdf

7.2 Alternate Method 2.Those Stage II systems subject to regulatory limitations on the dynamic back pressure between the Stage II riser and gasoline storage tank shall be tested using this methodology.

7.2.1 Disconnect the Stage II riser and install the "T" assembly as shown in Figure 3 below.

Figure 3

Capped "T" Assembly

See Figure at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP2_20080815_0819.pdf

7.2.2 Connect the nitrogen supply to the "T" assembly.

7.2.3 Open the nitrogen supply, set the delivery pressure to 5 psig, and use the flowmeter control valve to adjust the flowrate to lowest of the required nitrogen flowrates.

7.2.4 A pulsating gauge needle indicates nitrogen passing through a liquid obstruction in the vapor return plumbing. If this occurs, the cause of the liquid trap must be corrected.

7.2.5 The following information shall be recorded on the field data sheet, as shown in Form 2:

(a) Riser Number

(b) Gauge needle action

(c) Dynamic back pressure, inches H2O

Specified nitrogen flowrates and associated maximum allowable Dynamic Backpressures are included in Form 2.

7.2.6 Repeat subsections 7.2.3 through 7.2.5 at all required nitrogen flowrates for each and every riser.

7.3 Alternate Method 3.Those bellows-equipped Stage II systems subject to regulatory limitations on the dynamic back pressure at the nozzle/fillpipe interface during gasoline dispensing shall use the following methodology.

7.3.1 Assemble the Torus Pressure Test Assembly (Donut) as shown in Figure 4 below

7.3.2 Insert the nozzle spout through the inner hole of the donut.

7.3.3 Insert and latch the nozzle in the vehicle fillpipe. Visually insure that a tight connection is made between the donut and fillpipe.

Figure 4

Torus Pressure Test Assembly

See Figure at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP2_20080815_0819.pdf

7.3.4 Activate the dispenser, set the nozzle hold-open latch on low, and after at least one gallon has been dispensed start the stopwatch. Dispense a minimum of four gallons of gasoline.

Use the stopwatch to accurately time the dispensing rate. Record the total gallons dispensed and calculate the flow rate in gallons per minute. The following data shall be recorded on the field data sheet as shown in Form 3:

(a) Nozzle number and gasoline grade

(b) Gallons dispensed during test

(c) Maximum dynamic back pressure, inches H2O

(d) Minimum dynamic back pressure, inches H2O

(e) The average dispensing rate, gallons per minute

(f) Allowable backpressure range specified in the Executive Order

7.3.5 This Alternate Method shall only be conducted with the Stage I vapor poppet closed, since gasoline is being dispensed during the test.

7.4 Alternate Method 4.Those Stage II systems which utilize an incinerator shall conduct this test in conjunction with the applicable of Alternate Method 1, 2, or 3. This procedure verifies proper drainage of gasoline from the base of the vent pipe to the gasoline storage tank.

7.4.1 After verifying compliance with the dynamic back pressure standards, pursuant to the applicable of Alternate Methods 1, 2, or 3, close the Stage I vapor poppet.

7.4.2 Remove the pressure/vacuum (P/V) valve(s) from each vent pipe.

7.4.3 Carefully pour a minimum of five gallons of gasoline down each vent pipe.

7.4.4 Install the Vent Pipe Pressure Assembly as shown in Figure 5 below. Open the Stage I poppet(s) on all affected tanks.

Figure 5

Vent Pipe Pressure Assembly

See Figure at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP2_20080815_0819.pdf

7.4.5 Connect the nitrogen supply to the Vent Pipe Pressure Assembly.

7.4.6 Open the nitrogen supply and adjust the flowrate to 60 CFH.

7.4.7 After a minimum of thirty seconds, record the dynamic back pressure.

7.4.8 A dynamic back pressure, from the top of the vent pipe to the storage tank, of less than 0.5 inches H2O shall be considered acceptable.

7.4.9 Remove the Vent Pipe Pressure Assembly, carefully reinstall the P/V valve, and close the Stage I poppets.

8. REPORTING

8.1 Results of the dynamic back pressure test shall be reported as shown below:

8.1.1 Alternate Method 1 Use Form 1

8.1.2 Alternate Method 2 Use Form 2

8.1.3 Alternate Method 3 Use Form 3

8.1.4 Alternate Method 4 Include on applicable of Forms 1, 2, or 3

Form 1

Summary of Test Results

Dynamic Pressure Performance

See Form at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP2_20080815_0819.pdf

Form 2

Summary of Test Results

Dynamic Pressure Performance

See Form at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP2_20080815_0819.pdf

Form 3

Summary of Test Results

Dynamic Pressure Performance

See Form at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP2_20080815_0819.pdf

APPENDIX C

STAGE II POST TEST INSPECTION FORM

See Form at

http://www.registerofohio.state.oh.us/pdfs/3745/0/21/3745-21-10_PH_FF_A_APP3_20080815_0819.pdf

Effective: 08/25/2008
R.C. 119.032 review dates: 02/21/2008 and 08/25/2013
Promulgated Under: 119.03
Statutory Authority: 3704.03(E)
Rule Amplifies: 3704.03(E) , 3704.03(A)
Prior Effective Dates: 10/19/1979, 3/27/1981, 6/21/1982, 1/24/1983, 5/9/1986, 5/25/1988, 8/22/1990, 3/31/1993, 1/17/1995, 6/15/1999, 11/5/2002