DAQ-2024-011008

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DAQC-CI141190001-24
Site ID 14119 (B1)

MEMORANDUM

TO: FILE – GREEN NATURAL VENTURES LLC – Bullhorn Natural Gas Compressor
Station

THROUGH: Rik Ombach, Minor Source Oil and Gas Compliance Section Manager

FROM: Kyle Greenberg, Environmental Scientist

DATE: October 10, 2024

SUBJECT: FULL COMPLIANCE EVALUATION, Minor, San Juan County

INSPECTION DATE: September 11, 2024

SOURCE LOCATION: Remote location near Moab
San Juan County, UT 84532
DIRECTIONS: Leaving from Moab, take Highway 191 south bound towards
Monticello, turn left onto UT-46. Turn right onto CR 113/Lisbon
Road. Continue to follow CR-113 for 5.7 miles as it curves. Take
the Lisbon Valley Coal Mine Exit and continue for
approximately 7.5 miles. It is located on the northeast side in a
fenced area. The company has posted a sign on the entrance gate.

SOURCE CONTACTS: Ken Lapham
[e-mail]

OPERATING STATUS: Operating

PROCESS DESCRIPTION: The Bullhorn natural gas compression station is equipped with
two turbine powered compressor engine. The engines compress
and pumps liquid natural gas. The gas is delivered to the sales
pipeline. Natural gas is used to power the engines. The Bullhorn
Pumping Station is equipped with a control house that contains
monitoring equipment and a satellite down link so that the main
office can monitor and control the turbines through satellite
transmission.

APPLICABLE REGULATIONS: Approval Order (AO) DAQE-AN141190010-21, dated February
12, 2021; 40 CFR Part 60 Subpart JJJJ; 40 CFR Part 60 Subpart
HH; 40 CFR Part 60 Subpart OOOO

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SOURCE EVALUATION:

Name of Permittee: Permitted Location:

Green Natural Ventures LLC - Bullhorn Natural
Gas Compressor Station

600 Travis Street, Suite 5050 38.18173308 -109.1766821
Houston, TX 77002 San Juan County, UT 84532

SIC Code: 1311: (Crude Petroleum and Natural Gas)

Section I: GENERAL PROVISIONS

I.1 All definitions, terms, abbreviations, and references used in this AO conform to those used in the
UAC R307 and 40 CFR. Unless noted otherwise, references cited in these AO conditions refer to
those rules. [R307-101]

I.2 The limits set forth in this AO shall not be exceeded without prior approval. [R307-401]

I.3 Modifications to the equipment or processes approved by this AO that could affect the emissions covered by this AO must be reviewed and approved. [R307-401-1]

I.4 All records referenced in this AO or in other applicable rules, which are required to be kept by the owner/operator, shall be made available to the Director or Director's representative upon
request, and the records shall include the two-year period prior to the date of the request. Unless
otherwise specified in this AO or in other applicable state and federal rules, records shall be kept for a minimum of two (2) years. [R307-401-8]

I.5 At all times, including periods of startup, shutdown, and malfunction, owners and operators shall, to the extent practicable, maintain and operate any equipment approved under this AO, including
associated air pollution control equipment, in a manner consistent with good air pollution control
practice for minimizing emissions. Determination of whether acceptable operating and maintenance procedures are being used will be based on information available to the Director
which may include, but is not limited to, monitoring results, opacity observations, review of
operating and maintenance procedures, and inspection of the source. All maintenance performed on equipment authorized by this AO shall be recorded. [R307-401-4]

I.6 The owner/operator shall comply with UAC R307-107. General Requirements: Breakdowns. [R307-107]

I.7 The owner/operator shall comply with UAC R307-150 Series. Emission Inventories. [R307-150]
I.8 The owner/operator shall submit documentation of the status of construction or modification to
the Director within 18 months from the date of this AO. This AO may become invalid if construction is not commenced within 18 months from the date of this AO or if construction is
discontinued for 18 months or more. To ensure proper credit when notifying the Director, send the documentation to the Director, attn.: NSR Section. [R307-401-18]
Status: In Compliance. In compliance with all conditions of Section I.

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Section II: SPECIAL PROVISIONS

II.A The approved installations shall consist of the following equipment:
II.A.1 Compressor Station Plant Wide
II.A.2 Two (2) Compressor Engines Ratings: 1,170 hp and 1,380 hp (new) Fuel: Natural Gas Control: Oxidation Catalyst, each
II.A.3 One (1) TEG Dehydration Unit Rating: 30 MMscf/day
II.A.4 Two (2) Condensate Storage Tanks Capacity: 16,800 gallons (400 bbls), each
II.A.5 Two (2) Generator Engines Ratings: 325 hp and 301 hp Fuel: Natural Gas Control: Non-Selective Catalytic Reactor (NSCR), each
Status: In Compliance. There is one CAT 3516 LE compressor engine and one Caterpillar 3516 B compressor engine, a dehydration unit, two 400 bbl condensate storage tanks, and two natural gas fired CAT 3406 generator engines operating at this site. The dehydration unit is equipped with a 750k btu/hr reboiler. One of the storage tanks is equipped with a 500k btu/hr tank heater that is not operational. No unapproved equipment was observed.

II.B Requirements and Limitations
II.B.1 The Bullhorn Natural Gas Compressor Station Requirements: II.B.1.a The owner/operator shall not allow visible emissions from any stationary point or fugitive emission source on site to exceed 10 percent opacity. [R307-401-8] II.B.1.a.1 Opacity observations of emissions from stationary sources shall be conducted according to 40 CFR 60, Appendix A, Method 9. [R307-201-3] Status: In Compliance. Green Natural Ventures records reviewed by Ken Lapham do not show the visible emission opacity limits being exceeded. II.B.2 Stack Testing Requirement II.B.2.a The owner/operator shall conduct any stack testing required by this AO according to the following conditions. [R307-401-8] II.B.2.a.1 Initial Test The owner/operator shall conduct an initial stack test on the new 1380 hp Compressor Engine within 180 days after startup. [R307-165-2] II.B.2.a.2 Notification At least 30 days prior to conducting a stack test, the owner/operator shall submit a source test protocol to the Director. The source test protocol shall include the items contained in R307-165-3. If directed by the Director, the owner/operator shall attend a pretest conference. [R307-165-3, R307-401-8]

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II.B.2.a.3 Testing & Test Conditions The owner/operator shall conduct testing according to the approved source test protocol and according to the test conditions contained in R307-165-4. [R307-165-4, R307-401-8] II.B.2.a.4 Standard Conditions A. Temperature - 68 degrees Fahrenheit (293 K) B. Pressure - 29.92 in Hg (101.3 kPa) C. Averaging Time - As specified in the applicable test method [40 CFR 60 Subpart A, 40 CFR 63 Subpart A, R307-401-8] II.B.2.a.5 Access The owner/operator shall provide Occupational Safety and Health Administration (OSHA)- or Mine Safety and Health Administration (MSHA)-approved access to the test location. [R307-401-8] II.B.2.a.6 Reporting No later than 60 days after completing a stack test, the owner/operator shall submit a written report of the results from the stack testing to the Director. The report shall include validated results and supporting information. [R307-165-5, R307-401-8] II.B.2.a.7 Possible Rejection of Test Results The Director may reject stack testing results if the test did not follow the approved source test protocol or for a reason specified in R307-165-6. [R307-165-6, R307-401-8] II.B.2.a.8 Calculations To determine mass emission rates (lb/hr, etc.) the pollutant concentration as determined by the appropriate methods above shall be multiplied by the volumetric flow rate and any necessary conversion factors determined by the Director, to give the results in the specified units of the emission limitation. [R307-401-8] II.B.2.a.9 New Source Operation For a new source/emission point, the production rate during all compliance testing shall be no less than 90% of the maximum production rate (rated capacity) of the plant. If the maximum AO allowable production rate has not been achieved at the time of the test, the following procedure shall be followed: 1) Testing shall be at no less than 90% of the production rate achieved to date. 2) If the test is passed, the new maximum allowable production rate shall be 110% of the tested achieved rate. This new maximum allowable production rate shall be less than 90% of the allowed maximum production rate. This new allowable maximum production rate shall remain in effect until successfully tested at a higher rate. 3) The owner/operator shall request a higher production rate when necessary. Testing at no less than 90% of the higher rate shall be conducted. A new maximum production rate (110% of the new rate) will then be allowed if the test is successful. This process may be repeated until the maximum AO production rate is achieved. [R307-401-8] II.B.2.a.10 Existing Source Operation For an existing source/emission point, the production rate during all compliance testing shall be no less than 90 percent of the maximum production achieved in the previous three (3) years. [R307-401-8]

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II.B.2.b Test Methods When performing stack testing, the owner/operator shall use the appropriate EPA-approved test methods as acceptable to the Director. Acceptable test methods for pollutants are listed below. [R307-401-8] II.B.2.b.1 NOx 40 CFR 60, Appendix A, Method 7; Method 7A through Method 7E; or other EPA-approved testing method as acceptable to the Director. [R307-401-8] II.B.2.b.2 VOC 40 CFR 60, Appendix A, Method 18; Method 25; Method 25A; 40 CFR 63, Appendix A, Method 320; or other EPA-approved testing method as acceptable to the Director. [R307-401-8] II.B.2.b.3 CO 40 CFR 60, Appendix A, Method 10 or other EPA-approved testing method as acceptable to the Director. [R307-401-8] II.B.2.b.4 Volumetric Flow Rate 40 CFR 60, Appendix A, Method 2 or other EPA-approved testing method, as acceptable to the Director. [40 CFR 60, R307-401-8] Status: Out of Compliance. The previous owner Paradox Midstream failed to conduct the initial stack test on the Caterpillar 3516 B, four-cycle, rich-burn (RICE). Plate rated at 1380 hp Serial #AL700107 Compressor Engine in accordance to Method 25A Section 8.4, which is the required procedure of the calibration error test for the method to determine volatile organic compounds (VOC) emissions. The need for a required performance test to be conducted has been addressed in a compliance advisory. II.B.3 Stack Testing Limits II.B.3.a The owner/operator shall not emit more than the following rates from the 1,170 hp Compressor Engine: Pollutant lb/hr NOx 3.87 CO 0.78. [R307-401-8] II.B.3.b The owner/operator shall not emit more than the following rates from the 1,380 hp Compressor Engine: Pollutant lb/hr NOx 1.52 VOC 0.29 CO 1.83. [40 CFR 60 Subpart JJJJ, R307-401-8] II.B.3.c The owner/operator shall not emit more than the following rates from 325 hp Generator Engine: Pollutant lb/hr NOx 1.416 CO 2.834. [R307-401-8] II.B.3.d The owner/operator shall not emit more than the following rates from the 301 hp Generator Engine: Pollutant lb/hr NOx 0.66 CO 0.33. [R307-401-8] II.B.3.d.1 Compliance Demonstration To demonstrate compliance with the emission limitations above, the owner/operator shall perform stack testing on the emissions unit according to the stack testing conditions contained in this permit. [R307-165-2, R307-401-8]
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II.B.3.d.2 Test Frequency The owner/operator shall conduct subsequent stack tests within 5 years after the date of the most recent stack test. The Director may require the owner/operator to perform a stack test at any time. [R307-165-2, R307-401-8] Status: Out of Compliance. The 1,170 hp compressor engine, 325 hp generator engine, and 301 hp generator were all due for subsequent testing in July of 2024. A compliance advisory has been issued to address the failure to conduct subsequent performance tests on the engines. II.B.4 Compressor Engines and Generators Requirements II.B.4.a The owner/operator shall only use pipeline quality natural gas as fuel. [R307-401-8] II.B.4.b Stack height shall not be less than the following: Compressor Engines: 9.6 feet above the ground Electric Power Generator (325 hp): 12.0 feet above the ground Electric Power Generator (301 hp): 9.6 feet above the ground. [R307-401-8] Status: In Compliance. The stack heights appeared to be within the required limits. II.B.5 Condensate Storage Tanks Requirement II.B.5.a The owner/operator shall store only condensate and water in the condensate storage tanks. [R307-401-8] Status: In Compliance. Ken Lapham with Green Natural Ventures confirmed that the condensate tanks only store condensate and water. II.B.6 TEG Dehydration Unit Requirement II.B.6.a The stack height shall not be less than 14 feet above the ground. [R307-401-8] Status: In Compliance. The stack heights appeared to be within the required limits.
Section III: APPLICABLE FEDERAL REQUIREMENTS

In addition to the requirements of this AO, all applicable provisions of the following federal programs
have been found to apply to this installation. This AO in no way releases the owner or operator from any
liability for compliance with all other applicable federal, state, and local regulations including UAC
R307.

NSPS (Part 60), JJJJ Standards of Performance for Stationary Spark Ignition Internal Combustion
Engines

Status: Out of Compliance. The two (2) compressor engines and two (2) generator engines onsite need current performance test to be in compliance with the initial and subsequent performance test requirements of JJJJ.
NSPS (Part 60), OOOO: Standards of Performance for Crude Oil and Natural Gas Production,
Transmission and Distribution for which Construction, Modification, or Reconstruction Commenced After August 23, 2011, and on or before September 18, 2015 Status: Out of Compliance. Failure to replace the rod packing on the reciprocating compressor (JW unit 7399) every 26,000 hour or every 36 months, which is out of compliance with 40 CFR Part 60 Subpart OOOO § 60.5385. A compliance advisory has been issued to address this.
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MACT (Part 63), HH: National Emission Standards for Hazardous Air Pollutants From Oil and Natural
Gas Production Facilities

Status: In Compliance. The Bullhorn Natural Gas Compressor Station area source is not located in
a UA plus offset and UC boundary (as defined in § 63.761). The TEG dehydrator unit is not
required to control the unit’s process vents specified in § 63.765, the TEG dehydrator does not need
to monitor as specified in § 63.773, and the recordkeeping and reporting requirements specified in
§§ 63.774 and 63.775 are also not required. The optimum glycol circulation rate was determined in
2018 (see attachments).

AREA SOURCE RULES EVALUATION:

EMISSION INVENTORY:

Listed before are the Actual Emissions Inventory provided from Green Natural Ventures - Bullhorn
Natural Gas Compressor Station. A comparison of the estimated total potential emissions (PTE) on AO:
DAQE-AN141190010-21, dated February 12, 2021, is provided. PTE are supplied for supplemental
purposes only.

Criteria Pollutant PTE tons/yr Actuals tons/yr
CO2 Equivalent 14079.00
Carbon Monoxide 25.31 68.87
Nitrogen Oxides 32.72 275.6
Particulate Matter - PM10 2.39 0.88
Particulate Matter - PM2.5 2.39 0.88
Sulfur Dioxide 0.17 0.04
Volatile Organic Compounds 46.39 40.04

Hazardous Air Pollutant PTE lbs/yr Actuals lbs/yr
Acetaldehyde (CAS #75070) 1100
Acrolein (CAS #107028) 460
Benzene (Including Benzene from Gasoline) (CAS #71432) 1820
Formaldehyde (CAS #50000) 4460
Generic HAPs (CAS #GHAPS) 640
Toluene (CAS #108883) 871
Xylenes (Isomers and Mixture) (CAS #1330207) 260

PREVIOUS ENFORCEMENT
ACTIONS: Compliance Advisory (DAQC-582-23) - June 5, 2023
No Further Action (DAQC-005-24) - January 5, 2024
Compliance Advisory (DAQC-955-24) - September 25, 2024

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COMPLIANCE STATUS &
RECOMMENDATIONS: In regards to Approval Order (AO) DAQE-AN141190010-21,
dated February 12, 2021: Out of Compliance. The Bullhorn
Natural Gas Compressor Station is out of compliance with
Condition II.B.2.a.1, Condition II.B.3.d.2, 40 CFR Part 60
Subpart JJJJ, and 40 CFR Part 60 Subpart OOOO § 60.5385. A
Compliance Advisory (DAQC-955-24) was issued on September
25, 2024.

HPV STATUS: Not Applicable.

RECOMMENDATION FOR
NEXT INSPECTION: Confirm that stack tests have been conducted for all engines
onsite and that the rod packing has been replaced on the
reciprocating compressor (JW unit 7399).

NSR RECOMMENDATIONS: None

ATTACHMENTS: TEG Dehydration unit records.
MEMORANDUM
DATE: 30 August 2014
TO: Chrissy Schaffner, CCI Paradox Upstream LLC
FROM: Kevin Eldridge, Weston Solutions, Inc.
CC: Leann Plagens, CCI LLC
Josh Tuttle, CCI Paradox Midstream LLC
Blake Soyars, Weston Solutions, Inc.
W.O.NO.: 13844.062.002
SUBJECT: Applicability Determination of Subparts HH and HHH
CCI Paradox Midstream LLC and CCI Paradox Upstream LLC
BACKGROUND
Castleton Commodities International (CCI) operates several facilities located in the
Colorado and Utah Paradox Basin that contain equipment used for crude oil and natural
gas production, transmission, and/or distribution. This memorandum summarizes the two
federal regulations that may be applicable to such equipment and the compliance status of
the equipment located at the CCI facilities in Colorado and Utah.
REGULATORY REQUIREMENTS
On 16 August 2012, the United States Environmental Protection Agency (EPA) issued the
most current version of 40 Code of Federal Regulations (CFR) Part 63, Subpart HHH
-National Emission Standards for Hazardous Air Pollutants: Oil and Natural Gas
Production and Natural Gas Transmission and Storage (Subpart HHH) in the Federal
Register (FR). This standard was originally finalized on 17 June 1999 with corrections
issued on 29 June 2001 , 27 September 2001 , and 22 February 2002, with the final
proposed rulemaking initiated on 23 August 2011 .
EPA also promulgated 40 CFR 63 Subpart HH -National Emission Standards for
Hazardous Air Pollutants: Oil and Natural Gas Production Facilities in the FR on 17 June
1999 with corrections on 29 June 200 I and final updates on 3 January 2007. On 23 August
2011 EPA proposed new rulemaking for this standard. The following Sections discuss the
applicability of these two rules.
40CFR63SUBPARTHHH
This Subpart applies to major sources of hazardous air pollutants (HAP) I that:
1. transport or store natural gas prior to entering the pipeline to a local distribution
company or final end user, and
I Major sources of HAPs are sources that emit more than IO tons per year (tpy) of a single HAP or 25 tpy of
combined HAPs. See Attachment A for estimated potential to emit HAP emissions from each of the CCI
facilities.
2. contain a large or small glycol-based dehydrator unit (GDU) or units.
The only CCI facility in the Paradox Basin that is a major source of HAPs is Hamilton
Creek Compressor Station. However, Hamilton Creek is not part of the transport and
storage sector of the natural gas industry; it is part of the production sector. Therefore,
Subpart HHH does not apply to Hamilton Creek. This subpart does not apply to any of the
other CCI facilities in the Paradox Basin as they are all area sources of HAPs.
40 CFR63SUBPARTHH
40 CFR 63 Subpart HH applies to area and major sources that process, upgrade or store
natural gas. For major sources, the glycol dehydration units are the affected source
regulated, and for area sources, the triethylene g lycol (TEG) dehydration units are the
affected source regulated. Facility is automatically exempt from Subpart HH, if prior to
the point of custody transfer, with a facility wide actual annual average natural gas
throughput less than 18 ,400 standard cubic meter,s per day (m3/d) and a facility wide actual
annual average hydrocarbon liquid throughput less than 39,700 liters per day.
If the above exemption does not apply then dehydrator units are further categorized as 1)
those with an annual average natural gas flowrate less than 85,000 m3/d (equivalent to 3
million cubic feet per day MMscf/d) or benzene emissions less than 0.90 megagrams
(Mg/yr) (I .0 ton per year [tpy ]); and 2) those with an annual average natural gas fl ow rate
equal to or greater than 85,000 m3/day (3 MMscf/d) and benzene emissions equal to or
greater than O. 90 Mg/yr ( 1. 0 tpy).
TEG units are present at the following CCI Paradox Basin facilities :
• Lisbon Gas Plant (Lisbon)
• Bullhorn Compressor Station (Bullhorn)
• Hamilton Creek Compressor Station (Hamilton Creek)
• Andy's Mesa Compressor Station (Andy 's Mesa)
TEG units are not present at the Naturita Creek Compressor Station.
If the annual average natural gas throughput is greater than the 18,400 m3/d and a faci lity
wide actual annual average hydrocarbon liquid throughput is greater than 39,700 liters per
day the requirements of Subpart HH apply, but the facility may be exempt from the
emission control requirements provided:
• The actual annual average flowrate of natural gas to the glycol dehydration unit is
less than 85,000 m3/d; or
• The actual average emissions of benzene from the glycol dehydration unit are less
than 0.90 Mg/yr (1 tpy). This may be based on prior to controls, or after federally
enforceable controls.
With this exemption of Subpart HH, the facil ity must maintain records to demonstrate the
above. Table 1 summarizes the requirements for TEG units operated by CCI in the
Paradox Basin.
2
Andy's Mesa and Bullhorn
The dehydrators at Bullhorn and Andy's Mesa meet the· exemption of less than 1 tpy of
benzene emissions as the potential to emit from these dehydrators are less than 1 tpy of
benzene.
Lisbon
Lisbon is an area source. Subpart HH is applicable to the TEG Dehydrator at the Lisbon
Plant because the unit exceeds an actual throughput of 3 MMscf/d and emits greater than
one ton per year of benzene. This unit is considered an existing source as it commenced
operation before 8 Jul y 2005 . Also, the Lisbon Plant is not located in an Urban cluster
(UC), an Urban -1 County, or an UA plus offset and UC area. As such, no add-on
controls are required for this unit, and the Lisbon Gas Plant must determine the optimum
glycol circulation rate. This has been determined to be 306 gallons per hour.
Monitoringfor Lisbon
Lisbon is required to install and operate a continuous monitoring system to monitor glycol
circulation rate.
Recordkeeping Requirements for Lisbon
Lisbon is required to:
(a) Keep records of the results of monitoring; and
(b) Keep a record of the calculation used to determine the optimum glycol circulation
rate.
H a,mlton Creek
The original Hamilton Creek Title V permit application submitted to the Colorado
Department of Public Health And Environment (CDPHE), 2and the current construction
permit for Hamilton Creek show potential emissions of benzene that exceed 1 tpy.
However, the average actual emissions calculated using GRI-GlyCALC show that the
emissions do not exceed 1 tpy. Therefore, the Hamilton Creek dehydrator would be
eligible for the exemption listed above, as further demonstrated below.
The TEG # 1 glycol dehydrator located at Hamilton Creek is permitted with an annual
natural gas throughput limit of9,125 million cubic feet per year (MMscf/yr) (equivalent to
approximately 87,700 m3/d. However, the highest actual flow occurred in 2008 at 428.23
MMscf for the month of September. Using the highest month, the actual annual average
flowrate of natural gas to the glycol dehydrator was conservatively estimated at 14.27
MMscf/day (or 72 ,700 m3/day) which qualifies for the above exemption. In addition, the
highest actual annual average of benzene emissions (using 2013 data) was 0.15 tpy.
Although not required, Hamilton Creek meets both criteria to qualify for the exemption
listed in Subpart HH.
2 Hamilton Creek was listed as a major source of formaldehyde that is emitted from the compressor engines.
No other HAP emission exceeds the major source threshold.
3
Compliance Demonstration for Hamilton Creek
In order to continue to meet the criteria for an exemption from control requirements,
Hamilton Creek must document'the glycol dehydration unit's natural gas flowrate, or the
benzene emissions using the fo llowing procedures.
I) Actual Natural Gas flowrate:
• Install and operate a monitoring instrument that directly measures natural gas
flowrate to the glycol dehydration unit with an accuracy of plus or minus 2 percent
or better and convert annual natural gas flowrate to a daily average by dividing the
annual flowrate by the number of days per year the glycol dehydration unit
processed natural gas; or
• Document that the actual annual average natural gas flowrate to the glycol
dehydration unit is less than 85 thousand standard cubic meters per day .
2) Actual Benzene Emissions:
The determination of actual average benzene emissions from a glycol dehydration unit
must be made using the procedures listed below. Emissions shaJJ be determined using
either uncontrolled, or with federally enforceable controls in place.
• Determine emissions using the model GRI-GL YCalcrM , Version 3.0 or higher, and
the procedures presented in the associated GRI-GL YCalcTM Technical Reference
Manual; or
• Determine the average mass rate of benzene emissions in kilograms per hour
through direct measurement. Annual emissions in kilograms per year are
determined by multiplying the mass rate by the number of hours the unit is
operated per year.
Recordkeeping Requirements for Hamilton Creek
Records to demonstrate that the unit meets the exemption criteria of average flow or
benzene emissions must be maintained for Hamilton Creek. Based on the above analysis,
as long as the source continues to meet the actual annual average flowrate or benzene
emission criteria, Hamilton Creek will not subject to the emission standards of Subpart
HH.
CONCLUSION
Table 1 summarizes the Subpart HH requirements for the CCI Paradox Upstream and
Midstream operations. All the facilities are exempt from the requirements of Subpart HH
but must maintain records to demonstrate the exemption.
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Table 1. Subpart HH Requirements for CCI Paradox Midstream and Upstream Facilities.
Facility Name Dehydrator Emission Source Requirements
Unit Category
Lisbon Gas TEG Dehydrator Area The Lisbon Gas Plant is classified as an area source
Plant subject to Subpart HH. The actual glycol circulation rate
cannot exceed the optimum glycol circulation rate of
306 gallon per hour. See text for monitoring and
recordkeeping requirements.
Bullhorn Dehy I -Dehydration Area No specific permit conditions are listed for Bullhorn.
Compressor Unit -30 MMscf/day The Bullhorn permit application submitted in 2008
Station contained a model run showing the benzene potential to
emit emissions were less than 1 tpy therefore, the
Bullhorn facility is exempt from the requirements of 40
CFR 63 Subpart HH but must maintain records of the
benzene emission calculations.
Hamilton Creek Hanover TEG -25 Major See discussion in text. The Hamilton Creek facility is
Compressor MMscf/day classified as a major source for Subpart HH purposes.
Station However, it is exempt from control requirements of
Subpart HH since actual benzene emissions are less than
l tpy. Records of actual benzene emissions must be
maintained.
Andy's Mesa Natural Gas Dehydration Area Andy Mesa's permit exempts the facility from the
Compressor System using TEG -20 requirements of subpart HH based on potential
Station MMscf/day emissions of benzene being less than l tpy but must
maintain records of the emission calculations.
Naturita Creek No TEG Units Area Not subject to Subpart HH.
Compressor
Station
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ATTACHMENT A
HAP EMISS IONS
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Table 1. Bullhorn Compressor Station -Potential to Emit
Emission Unit Potential to Emit -Tons per Year (with controls)
NOx co voe S02 PM,JPNlu CH20 Other HAPS Total HAPS co,.
Eng 301 17.0 3.37 1.25 0.024 0.40 0.73 0.087 0.82 4,681
Eng 302 17.0 3.37 1.25 0.024 0.40 0.73 0.087 0.82 4,681
Eng 303 17.13 6.96 2.06 0.025 0.42 1.66 0.10 1.75 4,974
Gen-1 6.19 12.41 0.53 0.0065 0.22 0.090 0.051 0.14 1,296
Glycol Dehydrator 0.04 0.04 2.17 2.69E-04 3.41 E-03 3.37E-05 1.36 1.36 352
Condensate Tank 0.00 0.00 35.64 0.00 0.00 0.00 1.19 1.19 0.00
Total Existing 57.27 26.16 42.89 0.079 1.44 3.21 2.87 6.08 15,984
Gen-2 2.91 1.45 0.29 0.0060 0.20 0.032 0.083 0.11 1,200
New Total 60.18 27.61 43.18 0.085 1.64 3.24 2.95 6.20 17,185
Table 2. Andy's Mesa Compressor Station -Potential to Emit
I Controlled Potential to Emit (PTE)
Criteria (TPY) I .HAPs (lbs/yr) I I
TSP PM10 PM2.5 S02 NOx co voe , BZ Toi EB Xyl HCHO Acetal Aero n-Meth 224-
Equipment Description I Hex TMP
I
(I) Caterpillar 398 TA (625 HP) 0.24 0.24 0.0 14 17.7 2.41 19.37 I 21 19 53 9 362 0.42 0.42 53 1.1 12
Fugitive Emissions 9.30 I
(2) 400 bbl Condensate Tanks 21.46 I 120 40 4 12 206
NA TCO Process Flare 2.60 I
(I) Caterpillar G34 I 2 LE (580 19.6 2.00 4.80 I 16 1,000 158 97 42 95 HP) I
Caterpillar G35 I 6 LE (1,280 HP) 18.5 1.2 1.4 I 322
Caterpillar G3516 LE (1,280 HP) 18.5 1.2 1.4 I 322
20 MMSCFD TEG Dehy 2.00 I 2,014 602 210 218 68
I Permitted Sources Subtotal = 0 0.24 0.24 0.0 14 74.3 9.4 59.7 1 2,155 677 267 239 2,007 159 98 369 96 12
Total HAPs 3.04 /tnyl
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Table 3. Hamilton Creek Compressor Station -Potential to Emit
Controlled Potential to Emit (PTE)
Criteria (TPY) HAPs (lbs/yr)
Permit No PMIO PM2.5 S02 NOx co voe; BZ Toi Xyl HCHO n-224-Equipment Description
I Hex TMP
05SMOI IO RICE 0.45 0.45 0.027 17.1 4.40 1.60 I 1,778
05SMOl I I Generators (2) 0.13 0 13 0.0074 10.0 6.80 2.90 I
I 1,800
05SM0109 RICE 0.45 0.45 0.027 171 1.60 1.70 I l,778
05SM0106 Glycol Dehy 6.20 I 3,443 2,333 l,414 487
05SMOI78 Condensate Tanks 32.7 I
05SM0l79 Fugitive Leaks 6.30 '
Pcrmillcd Sources I.OJ I.OJ 0.060 44.2 12.8 51.4 I 2,JJJ 1,414 S,JS6 487 0 Subtotal = I 3,44J
Total HAPS 6.52 (tpy)
8
Table 4. Lisbon Gas Plant -Potential to Emit
Source Acetaldehyde Acrolein Benz Dichlorobenz Form Hexane Naphth Toluene Xylene
ID
E1* 0.03 0.03 0.04 0.54 0.01 0.01
E2 0.03 0.03 0.04 0.54 0.01 0.01
E3* 0.03 0.03 0.04 0.54 0.01 0.01
E4* 0.03 0.03 0.04 0.54 0.01 0.01
E4A 0.05 0.05 0.07 0.89 0.02 0.02
E4B 0.05 0.05 0.07 0.89 0.02 0.02
E5 0.03 0.03 0.04 0.54 0.01 0.01
E6 0.13
E7 0.13
E8 0.13
E9 0.13
E10 0.13
E11 0.13
E12 4.46E-04 2.55E-04 1.59E-02 0.382 1.30E-04 7.22E-04
E1 3 6.28E-04 3.59E-04 2.24E-02 0.538 1.82E-04 1.02E-03
E14 6.28E-04 3.59E-04 2.24E-02 0.538 1.82E-04 1.02E-03
E17 1.61 E-04 1.96E-04 2.48E-04 1.78E-05 8.59E-05 5.99E-05
E18 2.78E-05 8.55E-04 1.43E-04 3.10E-04 2.13E-04
E19 2.82-05 1.61 E-05 1.01E-03 0.0241 8.18E-06 4.56E-05
E21 1.9104 1.423 0.865
SUM 0.249 0.249 2.245 0.001 5.316 2.905 0.001 0.951 0.083
Total 12.0
HAPS
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File: J:\Project\Coitiply\TomBrown {Patara, EnCana, Lisbon)\Bullhorn 2010\JJJJfiZZ
;ZZ&HH RecQrds\DEHYl\Bullhorn Model Aggregate Rpt.txt 5/1/2008, 8:33:50AM
GRI-GLYCalc VERSION 4,0 - AGGREGATE CALCULATIONS REPORT
Case Name: Bullhorn Model Emissions
File Name: H:\Data\Midstream\Glycalc File3\Paradox\30 MMSCF_Bullliorn Model.ddf
Date: April 30, 200B
DESCRIPTION:
Description: 30 MMSCFD Glycol Dehydration Unit
Annual Hours of Operation: 8760.0 hours/yr
na-JISSIONS REPORTS:
CONTROLLED REGENERATOR EMISSIONS
Component Ibs/hr lbs/day tons/yr
Methane 0.0104 0.250 0.0456
Ethane 0.0144 0.345 0.0630
Propane 0.0235 0.565 0.1031
Isobutane 0.0115 0.276 0.0504
n-Butane 0.0259 0,620 0.1132
Isopentane 0.0105 0.253 0.0461
n-Pentane 0.0117 0.354 0.064 6
Cyclopentane 0.0016 0.036 0.0070
n-Hexane 0.0130 0.312 0.0569
Cycloiiexane 0.0294 0.706 0.1288
Other Hexanes 0.0124 0.299 0.0545
Heptanes 0.0271 0.650 0.1186
Methylcyclohexane 0.0265 0.635 0.1159
Benzene 0.1744 4 .186 0.7640
Toluene 0.0949 2.278 0.4157
Xylenes 0.0279 0.670 0.1223
C8+ Heavies 0,0019 0.046 0.0085
Total Emissions 0.5201 12.483 2.2782
Total Hydrocarbon Emissions 0.52 01 12.4 83 2.2782
Total VOC Emissions 0.4953 11.888 2.1696
Total HAP Emissions 0.3103 7.446 1.3589
Total BTEX Elmlssions 0.2973 7,135 1.3020
Page: 1
File: J:\py&Jj»ct\apBply\Toin Brown (PAti^ij^^nCajiai Lisbon}XBullhorn 20aO\J^JJ&ZZ
.Z2*HH R«cor<«\flEHXX\Sullbdim Hodel_Afli*l$«le-^^^ 5/1/2008, 8::?5:50AM
UVCONTROUfP BEGENERATOR EMISSIONS
CoSfVWlftXA Ibs/hr, lbs/day tons/yr
Methane 12 508 2 2827
Ethane 0 * 7222 17 332 3 1631
Piropane 1 .iw 28 783 5 2530
. . Isobutane 0.59a3 14 291 2 6081
n-Butane 1.350a 32 423 5 9171
Isopentane o;5^ 14 055 . 2 5651
n-P«ntane 0..8|^2-20 285 3 7020
Cyclopentane 0.0932 2 236 0 4081
n-Hexane o.siei 19 634 3 5832
CyclQhexane 2.0125 48 299 8 8145.
17 872 3 2617
Heptailes 53 ^0 -- 9 €816
Met hy 1 cyc iolie Jtane 2:4^2 53 501 9 7640
Benzene 12.52*9 300 597 54 8590
Toluene 245 132 . 44 7366
Xy Irenes 8.4298 154 314 28 .1624
C8+ IJeavies 175 •262 31 9853
Total Emissions
Tot»i.-Hyt^rOcacbon Emissions
Total voc Emissions
"SQtal HAP Emissions
Tiort^ BTEX Emissions
50.39^
49^1557
1209.576
1209.576
1179.736
719.678
700.044
220.7476
220.7476
215.3018
131.3413
127.7581
FLASH GAS a«£S6ICai8
Note: Fla^yb Gas Emissions are zero with the
Retryc^JBt/xecoinpression control c^c^iiiK^.
FLASH TAHK -OPF GAS
cotqpipnw^ lbs/day tons/yr
Jl^thane 26 678 4 8686
ethane 0.4112 9 870 1 8012
Propane 0,2995 7 187 1 3117
Isobutane 0;.TD^*2 2 260 0 4124
n-Butane O.i sir-' 3 610 0 6953
Isopentane 1 376 0 2511
n-Pentcine ».C698 1 580 0 2883
- •. V-v-Ki.
Page: 2
• '' * •, z:-%-
rifi J;-\#ro>*vt\Cpa«3ly\TqB Broim {P
.Z£«IU^Jle«M^^flC^ Model_Agq
na, Llsboiii^ \Bullhorn <2910\JJJJ&ZZ
.flpt.txt 5/1/2008, isSaVSOAM
• Cyclopjtntane 0 044 0 0081
n-^Hexane O.02f3& 0 804 0 1468
Cyclohexane 0 498 0 0908
\ . .> Other'Hexanes 0 978 0 1785 .
V-\ Z HBptanes o;.ft^[. 1 eio 0 1843
^j:\ift»^yl cy c lohexane 0 414 0 0756
> Benzene 0 401 0 0733 •
Ttfluane 0 199 0-. 0364.
Xylenes 0 046 0 0085^
- J... ce* Heavies
—^L.J-yjr —
0 279 0. 0508
Tptfti-JSjoissions "^•2'.a?5i. 57 434 10 4817
Hydjrocarboct Jfpds^xona 2,3911 57 434 ,10, 4817
Tptal VO^-iifcivicns 0.187^ 20 886 3. 8116
. Vbtal niU' f^eslons 1 451 0. 2648'.-.
To^l BffiX Emissions 0 647 . 0. Il80v.
1 ' •
CONGf NSERCOMBUSTION C^VICE
'Qf^ld^nsez: Outlet Teii?>eratuir«V^ 160.00 deg. F
Condenser Pres^^rA^
Condenser Duty:
^ ;pydflocarbon Recovery:
•• Produced Waterr
ABdolent Teaperaturfc
Excess Oxyg«»r_
Combustion Efficienaj(.*
12>50-.psia
l,«2e-001 MM BTP/hr.
1.96 bbls/day
rr^ 5.24 bbl»/d«y
: K 53. 00 deg. .F
. ' 4.00 * *
99-00 %
Su|fi|DlMMntal Fuel RequlrooMrnCr y\e2e-001 m BTU/hr
'•f .'
Cc»is>DRent Enltj^Ad- Destroyed
Methane
Ethane
Propane
Isobutane
n-Butane
Isopentane
n-Pentane
Cyclopentane
n-Hexane
Cyclohexane
2.00% 98.00%
. 1.99% 98.01%
L.96% 98.04%
1.93% 98.07%
.1.91% 98.09%
•1.80% 98.20%
•^^.74% 98^6%
.'^1,71% 9ft.5?%
^1.59% 98.41%
-^-;i.+6% 98.54%
.-.tr
Page: 3
• ZrZ'-Z'
J:A?^*'C^\<>*^y\''oia Brown (Pataapi^^lfca^Cana, HsboB) XBulli^iji .2p-10\JJJJiiz
WotttVsitftlK&ullluM: Model AwtwiWIg Rpt.tKt 5/X/209S, 8;^.'^AH
i' other Hexanes - .-•1.67% 98.33%
Heptanes 1.23% 98,77%
methylcyclohexane t . .1.19% 98.61%
-Benzene •. .*^*1.39% 98.61%
Toluene ' •0.93% 99.07%
Xylenes • ji3.43% 99.57%
C8+ Heavier , * :o.03%
^ i: S-
99.97%
ABsonna
MOTE': »ecau«e^tS«i Calculated Absorber Sta^iNi was below the minimun
allowwtt GRl--^YC»l!g; has a&t the nuraber oiC-ftbsorber St-ages to 1.23
ind haji/calctilated a • revised Dry Gas D*y .|it>int.
• Calculated Absorber Stages: 1.25
Calculated Dry fias Dew Point: / 3-46 lbs. H20/l«SCF •• , - 1^. •, • • • ' ••
'., • Teffiperaturej
Pxessuret
Dry Gas Flow Rate*
, • ^^Gl^rccl Losses with Dry Gasi-
• Wet Gas Water Content; J|||turAted
Calculate Wet Gas Water Content; 67.77 lbs. H20/MHSCF
Calculatad te*ti. Glycol Recirc. Ratipi' 4.4? gal/lb H20
53.0 deg. F
132.0 psig
30.0000 *fflSCF/day
0.0116 Ib/hr
Coi^>onent
Pen^lning
:i>ry Gas
r
Absorbed
in Glycol
Water 5 .09% 94. 91%
Carbon Dioxide 99 .92% 0. 00%
Nitrogen too .00% 0. 00%
Methane • 100 .00% 0. 00*
Ethane .98% 0. 02%
Propane 99 .96% 0. 04%
Isobutane . .92% 0. 08%
n-Butane . 99 .89% 0. 11%
Isopentane ^9 .85% a. 15%
n-Pentane . 99 .80% 0. 20%
Cyclopentane : 99 .18% 0.. 82%
n-Hexane V vf99 .55% 0. 45%
Cyclohexane ' .••.••38 .12% . 1. 88%
other Hexanes • 99 .69% 0. 31%
Heptanes 98 .86% I. 14%
methylcyclohexane .22% 2. 78%
Benzene 81 .97% 18, 03%
Toluene *9 .41% 30. 59%
Xyl enes >» .76% 61. 24%
5 ij?
' "tP
• P«ge: 4
File: J:\Project\Comply\Tom Brown (Patara, EnCana, Lisbon)\Bullhom 2010\JJJJ&ZZ
,ZZ&HH Records\DEHYl\Bullhorn Model Aggregate Rpt.txt 5/1/2008, 6:33:50AM
C8+ Heavies 95.93% 4.07%
FLASH TANK
Flash Control: Recycle/recompression
Flash Temperature: 110.0 deg. F •
Flash Pressure: 45,0 psig
Component
Left in
Glycol
Removed in
Flash Gas
Water 100 00% 0 00%
Carbon Dioxide 86 22% 13 78%
Nitrogen 31 16% 68 84%
Methane 31 92% 68 08%
Ethane 63 72% 36 26%
Propane 80 02% 19 98%
Isobutane 86 35% 13 65%
n-Butane 89 49% 10 51%
Isopentane 91 13% S 87%
n-Pentane 92 81% 7 19%
Cyclopentane 98 07% 1 93%
n-Hexane 96 08% 3 92%
Cyclohexane 99 01% 0 99%
Other Hexanes 94 86% 5 14%
Heptanes 98 14% 1 86%
Methylcyclohexane 99 26% 0 74%
Benzene 99 87% 0 13%
Toluene 99 93% 0 07%
Xylenes 99 97% 0 03%
Ce+ Heavies 99 86% 0 14%
REGENERATOR
No Stripping Gas used in regenerator.
Component
Remaining
in Glycol
Distilled
Overhead
Water 38.59% 61.41%
Carbon Dioxide 0.00% 100.00%
Nitrogen 0.00% 100.00%
Methane 0.00% 100.00%
Ethane 0.00% 100.00%
Propane 0.00% 100.00%
Page: 5
me; if^t&^t \QDBplyVToBb Brown (P ana, Li^Jrori) \Bullhpr?\:*<J10VJJJiJ622
« Rpt.txt 1/1/20'OjS, ffi;33*5CW4
Isobutane
n-Butane
isopentane
n-Pentane
Cyclcjjentajie
n-Hexanc
Cyclohexane
Other Hexanes
• Heptanes
Methylcyclohexane
Beoaene
Toluena
.Xylenes
Ce.+ Heavies
fl.00%
Tp..00%
••••'^.•54%
• 0.51%
0.52%
3-23%
.1,05%
. 0.51%
'4-03%
5.91%
r^ia.91%
,JUt,04%
100.4)0%
100.00%
99.45%
99.46%
99.49%
99.48%
96.77%:
98.951.
99.49%
95.97%
94.99%
9?i0^
87.09%
87.961
STREftH REKifi^r ...
MET <^ S*I?B£AH
Flow Rat*^'
53.00 deg. F
' 1-46.70 psia
1..25e+00€ acfh
CQnc>
''^Tita%)
Loading
(Ib/hr)
Water l'.4*iii-001 8.49e+001
C^yrbon trioxide 1.^83*^-001 2.66e+002
Nitrogen 4V^3SH'O00 4,46e+003
Methane 8-3^»y001 4.44e+004
Ethane 6.74«*0(J0 6.69e+QQ3
. „ Propane.2v-<lfl*000 3,51e+003
Isobutane 4.59iH>01 B.eOe^-OOS
. n-Butane 6.>7«rOOl 1.34e+003
Isopentane l-ftla-^OOl 4.33e+.O02
.•ifr- n-Pentane 1.91q(^001 4.54e+O02
' Cyclopentane 5.006-003 l.iee+001
n-Hftxane 6.70»-002 1.90e+002
.• Cyclohexane 3.90*'002 1.08e+002
Other Hexanes 8.i79»r0O2 2.50e+002
Heptanes 6-t>0|4^0O2 1.9ee+002
Methylcyclohexane 2.5^,002 8.09e+001
Benzene 2,70B*-002 6.95e+001
Toluene l..t0j»-002 3.34e+00l
• 1 'hi-
Z^ ':^^
J'1'..'Z'
Page: 6
File: J:\S%*4fiP*^VC**e»ly^Tao. Brown (P»
.ZZtHK B«coTiittfWHY,l>BuIlhom Hodel_j
a, Lisbpn^ \B«^lbom 2010\JJJJs2i
Rpt.txt 5/1/2003, r:3:3i*0AM
Xylenes 3.00».-003 1.05e+001
C8+ Heavies 3.2*«^()02 1.80e+002
TOt«r'cort53onents lOCf.OO 6.36e+O04
DRY GA3 'STREAM
Tejapera1:i^e:
PressureJ
Flow Rate:
53.00 deg. F
146,70 psia
1.25e+0Q6 scfh
Coa^nent Loading
(Ib/hr)
Water 1.299-^03 4.32e+000
Carbon Dioxide 1.8^#«*01 2.65e+002
Nitrogen 4;«.*»S300 4.46e+603
Methane 8:3i*0+OOl 4.4 4e+004
Ethane e.T'Si^iSBOO 6.69^+003
Propane 2.41^*00 3..50e+003
Isobutane 4,59*W001 ^^79e+002
n-Butane S^li^^l 1.33e+003
Isopentane 1.82KP*ftRH 4.326+002
n-Pentane 1.91*^1 4.54e+002
.Cyclopentane 4.9fie»s603 1.15e+001
n-Hexane 6.69^002 1.90?+002
Cyclohexane 3iaS*j(ip02 1.06e+002
othar Hexanes 8;78«'*i>02 2.4 9e+002
.. ' Heptanes 5.94**002 1.96e+002
.t4etbylcyclohexane 2.f3«-002 7.87e+001
nrnrrm Mjj^pr? 5.70e+001
Toluene 1.90^^03 2.32e+001
Xylenes 1,16»^D3 4.07e+000
C8+ Heavies 3^J0iW^2 1.72e+002
Total Components 00 .6.35e+004
LEAN -SLYCOL JrtWyftl
— -1—
TsMp^raturer' ''^-•.53.06 deg.
Flow Ratf': 5.99e+000 gpm
Comppnent ,Coae:. Loading
(Ib/hr)
TEG 9.'84W01 3.32e-t-003
Water 1.50»+000 5.06«+001
Carbon Dioxide 6.13«:rfll3 2.07e-011
Page: 7
• - 'v • -
"•^•.^t^m~....
File- J:\Proj««t\e<»plyVJo« Brown (P<^4.^j[teC«.a, Li,»>on>«uUhom ?010\JJJJ«Z
Nitrogen 4.79e*-til3 1.61e-011
. . Methane 1.63r*'ftlfl 5.48e-017
Ethane
Propane
Isobutane
n-Butane
Isopentane
n~Pentane
'Cyc1opentane
n-Hexane
Cyclohexane
other Hexanes
1.59a-008
1 *8 le-^
6-I3«!ftlO
lv|jMH)09
9i>ll*?»S)05
l<3A^t»Q4
1.42<lHrfi05
1.27*'^04
1.9«^pW)3
2*3.55^r:004
5.35«-007
6.10e-008
2.07e-008
3.7 4e-00e
3.23e-003
4.586-003
4.77e-004
4.28e-003
6.72e-002
7.93e-003
Heptanes 3.36*i.004 1.13e-002
Methylcyclohexane 2.j.ia«*003 9.36e-002
Banzene 1.^6«i-^002 6.60e-001
Toluene 2.M|W002 8.77e-001
Xylenes 2"."f3^002 9.53e-001
.CB-t- Heavies 2..M^Ct2 9.99e-0Dl
Total Components. 106.00 3.37e+Q03
-t
RICH GLTqpoi." STREAM
Teaif^rliHtpre: 53.00 deg. F
^E««fbf^-. 1.46.70 psia
nW^MMret^ .-.6..27e+0p0 gpm •
IlOTI^V^I&t^am^ws morei than one phase-
.Conponent
. TEG. 9.=r6*t001
Water 3,.l4yi(»O00
carbon Dioxide 5.Sijfc0.03
Nitrogen 4>|tfl|r<J03
Methane t'.j&fliiit^02
Loading
{lb/hr.>
3,32e+003
1.31e+002
2.07e-001
1..63*-001
1.63e+000
Ethane St3»rQQ2 1.13e+000
Propanf!.. Hjnm' HP" 1.50cf^00
Isobutane lSy^^02 6.90e-001
n-Butane 4-.3t*.-002 1.51e+O0O
Isopentane l.J*gk*<ia2 6.46e-00i
n-Pentane 4^iiN«>2. 9.16e-001
cyclopentane 1|i3Fj%003 9.55e-002
n-Hexane jfeT44#002 8.56«-001
Cyclohexane 5,.^«-002 2.IO0+OOO
other Hexanes 2.^/^2 7.93e-001
IS
"rC-Page: 8
•tii
File: J; \Proj*p$:.\.Conply\Ton Brown [gat'i<j^ig^seana, Lisbon) \Bu^lho|rn; ;»01P\JJJJfcZZ
•"Tfmi.m riu'HrTn'i'nimiifii i tr iiii„Ttjji'(iflWtf Rpt.txt 5/i/2oo6, 8:31:50AH
H»ptanes 6.4ieiM?002 2.26e+000
M4tJ]tylcyclohexane 6..68#^b02 2.34e+000
Benzene 3..77.«^0l 1.32e+001
Toluene 3.£744*01 l.lle+001
Xylenes 2^jHiji^01 7.36e+000
C8+ Heavies'2.3.7^^1 8.3le+000
Total Components' t'^^l.QP 3.51e+003
FLASH/TAH OFT GAS STR£AH
Temperature;
Piefssure;
Flow'itate;
110.00 deg. F
. 59.70 psia
3'.90e+001 scfh
Component
i.\^i—..
Cow?i. Loading
(Ib/hr)
.•f'iz:.
Water. 1,92*^1 3.55e^3
Caxbon Dioxide S.aOffOOl 2v85«-002
Nitrogen 3.i^t0^DO 1.12e-001
Methane 6.,74««(|t01 l.lle+OOQ
Ethane 1.3l3#i|irtn 4.11e-0Ol
Propane 6.,i$l«<^0O 2.99e-*001
lisobutane l^Se!«^00 9.42e^002
. n*Butane 2,«a|i9iO 1.59e-001
:;.,.ISop«ntane 7.Tf3(yjj001 5.73a-*002.
'jiTPentane 8.»7»r001 6.58e-0Q2
Cyclopentane 2-;3t£i|^KH)e 1.84e-003
n-Hexane 3.78!fe^01 3.35e-002
. Cyclohexane '2'i4pi|hfOQl 2 ..076-002
Other Hexanes 4.6k)tr^01 4.08e-002
Heptanes 4";08ie*001 4.21e'-002
Methylcyclohexane I.Ti;
Benzene 2.
Toluene 8,
Xylenes l^Tfif^Ol
C8+ Heavies r^4^|iih}^2
¥^t#l'Conunents ' .t^^O 2.54e+O00
01 i.73e-002
1 1.67e-002
8.30e-003
1.94^-003
1.16e-002
r^jisn TANK'OII^I STRE^'.
'CjW^r;^'^* 110.QQ d«g. F
. .''l9.i3M'J^Kt4:.. „ 6.ir^-i-000 gpct
onent leading
7^ Page: 9
File: >>:\Pr<Sf^\Co*splyV?tttt Brown ^nCana, llabon) \8wjU*»oni 2010WJJJi2Z
Rpt.txt '5/1/2008, 8i33:50AM
t«t%) (Ib/hr)
TEG 9.*7j#4.001 3.32e+003
Water 3.7441^0 1.31o+002
Carbon Dioxide 5.9^^*003 l,78e-001
Nitrogen 1,.45^003 5,07e-002
Methane l.*.94-f02 5,21e-001
Ethane-2.0*f4D.02 7,22e-O01
Propane 3.4Z<(.*ob2 1.20e+O0O
Isobutane l^>0ffr!802 5,95e-001
n-Butane 3,'e6«'002 l,35e+000
Isopentane l:«lj»-jp02 5.e9e-001
n-Pentane 2.*3#r*002 8.50e-001
Cyclopentane 2.eT««003 9.37e-002
n-Hexane 2.35Wtj002 6.22»-00l
Cyclohexane 5.94i|I=-C02 2.08e+000
Other Hexanea 2.a5*iffl02 7.536-001
Heptanes. 6.14ift^02 2.22e-f000
Methylcyclohexane G^^Si^^Z 2.32e+000
Benzene 3.7^001 1.32e+001
Toluene 3.r7.«^001 l.lle+OOl
Xylenes 2.11:**^01 7.38e+000
CB-f Heavies 2^X11^01 8.30e+000
Total Components '. l^^&O 3.50e+003
FLASH GA5- tHtSSI0«S
Cotitrol ffethpd: R«cycle/recompr*M4on.
Control ECy^Ciency: ' 100.00 ' :- .r
' •• ."ij
Note: Fift^ Sas-ftnissions are zero yitfcthe
Rs«^i4tl«/reconipression control,^|^'on.
REGENERATOR OVEBHSADS STREAM
Temperfti^t*:
Fldft'liftt*:
212.00 deg. F
14.70 psia
l.93e*003 scfh
Conijonent
•4*iJ*)
Loading
(Ib/hr)
Hater ftj*€l»tO01 S.QSe+OOl
CAtbon Dioxide ?>.*tt*^002 1.7ee-00l
Nitrogen 3.5**K>e2 5.076-002
Methane 6.40iip-001 5.21e-001
Page: 10
File: J:\pjris?H*iet\Oeaiipiy\Twa Brown (P»t#«^.
;S^HH R«COK$»Sftiwftai«W^orn Motiel^Ai
na, Lirt5on}\pullbom 20lO\JJJJ4Zt
l^t.cxt 5/1/20M, 8:3^.50AM
Ethane 4.73«-p.01 7,22e-00l
Propane 5;36«':0Q1 1.20e+000
Isobutane 2;fi4e-*fi0}. 5,95e-001
n-Butane 4*5»«rt)01 l,3.5e+000
Isopentane l.tOft^l 5.86e-001
n-Pentane 2.3l**<)0l 8.45e-001
Cyclopentane 2,-6^^02 9,32e-002
. n-Hexane 1.87#**01 8.l8e-001
Cyclohexane 4iH*^ftl 2.01e+000
Other Hexanes l.TOfc^iOOl '7.456-001
Heptanes 4.34Vr*:001 2.21e-f000
«ethylcyclohexane 4.*7«tp01 2.23e+000
Benzene 3.l6^|f&(W 1.2.5e+D01
Toluene 2,l8<(*O00 1.02fi+001
Xylenes l.lr9«+000 S.43etOOO
C9+ Heavies B,44flH0Ql 7.30e+000
Total Cosponenta iOtt'.OO 1.31a+002
CONnENSpfrJ|t6©0CE0, IJATEp STREAM ——
X«npf)$atura': . 160.00 deg. F
Flo* Itate: .ll53e-001 9pm
CoiitK>nsnt Coae, Loading
tlb/hr) tpprU
Water 9.99^V001 7. ,64e+0Ql 999078,
- Carbon Dioxide 3.*9ft^004 2, .74ft--004 4.
Nitrogen 3.48^06 2, .€6e-•006 0.
Methane. 6.28#j,095 4. .80*' •005
Ethane 9.)4*f^05 7, .07e--005 1.
Propan^ t'* ^.l^»^04 1, .4 6fe-•004 2.
Isobutane 3, ,74«-O05 O.'
n-Butane l.j|«|^04 1, .07e-•004 1.
Isopentane, 3j»9«^005 2, .90fe-'OOS 0,
n-Pentane 5,57*.005 4 .26e--005 1.
Cyclopentanft 2 .84e--005 0. ^
n-Hexan« 3;7ftSp05 2 .e9e--005 0.
Cyclohexane 4.2S«-^04 3 .26e-'004 4.
Other .Hexanea 3.00>-^Q& 2 .29e--005 0. '
Hftptanes 4;'17»H}0S 3 ,19e-'005 0,
N«thy1oyclotw vane I>1»»«004 1 .36c--004 2.
Siif94^O02 4 .50e--002 589.
Toluene 2,|>*IJt002 1 .89e-•002 247.
Xyian«a 6.aim^.oo3 5 .26e' '003 69.
C8+ Heavies 8. l9»-i0O7 6 ,25e--007 0.
.
'A- •• -
H^r,':
Page: 11
File: 4;\P i^l^tom Brown (Pat«jf|j|(^JnGana> LisbonABuUhom 20ZO\JJJJ6ZZ
ll^lhom Model_Aqflft^^M»«. Rpt.tj^t 5/l/2doe, e:33sflOfttt
Tatal Conpoitents lOfi'.OO 7.e4e+001 lOOOODO.
COItDENSER i^CeOffWD OIL STREAM
Ten^jerature; 160^00 deg. F
Plow Rate; 5n2e-O02 gpflft
Component Loading
<lb/hr)
Water 5.W4W1L0Z 1.42e-002
Catrboh Dioxide l.T6«r^I03 4 .28e-O04
Nitrogen 2.90m^Qi 4 . B7B-^05
Methane 1 ^74«^^ - 4,22e-004
Ethane .l,23l4Wttq2 3.01fe-G01
Propane 9.Q7ft-p02 2.21e-002
Isobutane 8.-(a%ri002 1.97e-002
n-Butane 2.«J**.0ai 5.83e-002
Isopentane 2.4i«-e01 5.93e-002
n-Pentane 4.44e*-O0l 1.08e-001
Cyclopentane 5,56«Te02 l,35e-0O2
n-Hexane 6.93*V001 1.69e-001
Cyclohexane 2.23«*C00 5.42e-O01
Other Hexanes 5.^-001 1.23e-00l
Heptanes 3.52ei;D00 8.560-001
Methylcyclohexane 3.72flr*OO0 9.06e-001
Beniene 1.54eJ^0Bl 3.76e-t000
Toluene 2,^fti001 5..45e+fl00
Xylenes 2.<Wj|»*<K)l 5.03c-fC(00
C8+ Heavies 2.96(|i#troi 7.21«-f000
Total Components XCFb^OO 2.43s-f001
CONDENSER VK«T STREAM
Tefl^r*tttt»:.
Pressure'.
Flow Rate^
160.00 deg. F
12.50 psia
2.30e+002 scfh
Companent CnK- Loading
(Ib/hr)
Hater 3.79»+xbl 4.14e+000
Carbon Dioxide 6.67eA301 1.7ee-00l
Nitrogen 2..»8»H301 5.06e'6Q2
Methane 5.16**000 5.21e-001
Ethane 3.95lf>C00 7.19e-001
Pagp: 12
• <•
File: ^l|;W(flsiict\$q|^yVtOT Browp (PAtapa^..-EnCana, t^lsbon)'vBullhom 2010\JJJJ&ZZ
igwy^liL!»qo<^ Model_Aggjp»q*<V Rpt.txt 5/1/2008, B:33:50AM
Propane 4^^14^000 l.lBe-t-OOO
Isobutane It-^itm^QO 5.76e-001
. n-Butane 3iM|i4JW)l0 1.29e-K000
Isopentane' I. ^QiflKidO 5.26e-001
n'-Pentane l.«9#»>000 7.37e-001
Cyclopentane l.*'%r>001 7.96e-002
n-Hexane l*2Mr4^00 6.49e-001
Cyclohexane 2.<H|nN>00 1.47e+-O00
Other Hexanea lilSnWOO 6.22e-001
Heptanes 2.236+000 1.35e•^000
>l«thylcyclohexane-2^|^2«M)00 1.32e-f000
Benzene l.d4f^01 8.72e-(-000
Toluene 8., S<3ii!#rOOO 4.75e+000
Xylenes' 2.^,.i7f^'000 1.40e+000
C8+ Heavies »,lti^02 9.67e-002
Total Components 100.00 3.04e+O01
COMBUSTION • DEVICE OFF GAS STREAM
>_
rratur^i^-^ 1000.00 deg. F
Rr*a»ur^^ ' 14,70 psia *'
Lot*"Rate;..- 2.81e+000 scfh '
:.--rfcoB$»onent Copc^. Loading
1^*-) , (Ife/hr)
/•i/- '"'"^ Methane S/lflSKWO 1.04(9^002
Z Ethane 6,f^fiJ0"0 1.44e-002
•V Propane 7.^fe000 2.35e-002
Isobutane 2^wBfO00 1.15e-002
n-Butane 6...^1.<^ftf00 2.59e-002
.Isopentane
n-Pentane
Cyclopentane
n-Hexane
Cyclohexane
Other Hexanes.
Heptanes
Methylcyclohexantf
,/ Benzene
Toluene
3^.r«0^)oa
1.4}9i|irDoi
)v3<!|^001
1.05e-002
1.47e-002
1.59e-003
1.30e-002
2.94e-002
1.24e-002
2.71e-002
2.65e-002
1.74e-001
9.49e-002
^ ^- Xylenes l.-Sf^OOO 2.79e-002
.^'; C8+ Heavies- l.,«54»^001 1.93e-003
o "^Otal Components . iflO.OO 5.20e-001
Tage: 13
Z -'ife
Page: 1
GRI-GLYCalc VERSION 4.0 -AGGREGATE CALCULATIONS REPORT
Case Name :
File Name: H:\Projects\ENV\Paradox Resources\2018 Reporting\Working\Utah Oil and Gas
Emission Inventory -Due April 15\Bull Horn CS Dehy.ddf
Date: April 13, 2018
DESCRIPTION:
Description:
Annual Hours of Operation: 8700.0 hours/yr
EMISSIONS REPORTS: 5.4343 lb/hr voe + o.1957 lb/hr voe = 5.6300 lb/hr voe
UNCONTROLLED REGENERATOR EMISSIONS -------------------------------------------------------------------
Component lbs/hr lbs/day tons/yr
------------------------------------------ ----------- -----------
Methane 0 .1505 3.612 0.6547
Ethane 0.1434 3.441 0.6236
Propane 0.3102 7.444 1. 3493
Isobutane 0 .1696 4.070 0 .7377
n-Butane 0 .2379 5 .708 1 .0347
Isopentane 0.1632 3.916 0.7097
n-Pentane 0 .2156 5.175 0.9380
n-Hexane 0 .0697 1.672 0 .3031
Other Hexanes 0.0427 1.024 0.1856
Heptanes 0.2558 6.140 1.1129
Benzene 0 .3943 9.464 1 . 7154
Toluene 0. 7114 17.074 3.0947
Ethylbenzene 1.2269 29 .447 5.3372
Xylenes 1. 6370 39 .287 7 .1208
------------------------------------------ ----------- -----------
Total Emissions 5.7281 137.475 24.9173
Total Hydrocarbon Emissions 5 .7281 137.475 24 .9173
Total voe Emissions 5.4343 130 .422 23 .6391
Total HAP Emissions 4.0394 96.945 17.5712
Total BTEX Emissions 3.9697 95.272 17.2681
FLASH TANK OFF GAS
Component lbs/hr lbs/day tons/yr ------------------------------------------ ----------- -----------Methane 0.3416 8.197 1. 4858
Ethane 0 .0905 2 .173 0 .3938
Propane 0 .0840 2.017 0.3656
Isobutane 0.0297 0. 712 0.1290
n-Butane 0.0310 0.743 0.1347
Isopentane 0 .0181 0 .434 0 .0786
n-Pentane 0.0188 0.452 0.0819
n-Hexane 0.0033 0.079 0.0143
Other Hexanes 0 .0027 0.064 0. 0117
Heptanes 0 .0058 0 .138 0 .0251
Benzene 0.0006 0.014 0.0025
Toluene 0 .0006 0 .015 0 .0028
Ethylbenzene 0 .0006 0.015 0 .0027
Xylenes 0.0006 0.013 0.0024
Page: 2 ------------------------------------------ ----------- -----------
Total Emissions 0 .6278 15 .066 2 .7308
Total Hydrocarbon Emissions 0.6278 15.066 2.7308
Total voe Emissions 0 .1957 4.696 0.8512
Total HAP Emissions 0 .0057 0.136 0 .0247
Total BTEX Emissions 0 .0024 0.057 0.0104
EQUIPMENT REPORTS:
ABSORBER
NOTE: Because the Calculated Absorber Stages was below the minimum
allowed, GRI-GLYCalc has set the number of Absorber Stages to 1.25
and has calculated a revised Dry Gas Dew Point.
Calculated Absorber Stages:
Calculated Dry Gas Dew Point:
Temperature:
Pressure:
Dry Gas Flow Rate:
Glycol Losses with Dry Gas:
Wet Gas Water Content:
1.25
6.50 lbs. H2O/MMSCF
90.0 deg . F
400 .0 psig
3.9000 MMSCF/day
0.0144 lb/hr
Saturated
Calculated Wet Gas Water Content: 89 .69 lbs . H2O/MMSCF
3.00 gal/lb H2O Specified Lean Glycol Recirc. Ratio:
FLASH TANK
Component
Water
Carbon Dioxide
Nitrogen
Methane
Ethane
Propane
Isobutane
n-Butane
Isopentane
n-Pentane
n-Hexane
Other Hexanes
Heptanes
Benzene
Toluene
Ethylbenzene
Xylenes
Remaining
in Dry Gas
7 .24%
99 .88%
99 .99%
99.99%
99 .97%
99 .94%
99 . 91%
99.88%
99 .86%
99 .82%
99.67%
99 .75%
99 .32%
88.20%
81. 96%
73 .01%
63.99%
Absorbed
in Glycol
92.76%
0 .12%
0.01%
0.01%
0.03%
0 .06%
0.09%
0.12%
0.14%
0 .18%
0.33%
0 .25%
0 .68%
11. 80%
18.04%
26.99%
36.01%
Flash Control : Vented to atmosphere
Flash Temperature: 105.0 deg. F
Component
Flash Pressure: 130.0 psig
Left in
Glycol
Removed in
Flash Gas
REGENERATOR
Water
Carbon Dioxide
Nitrogen
Methane
Ethane
Propane
Isobutane
n-Butane
Isopentane
n-Pentane
n-Hexane
Other Hexanes
Heptanes
Benzene
Toluene
Ethylbenzene
Xylenes
100.00%
85.89%
29.93%
30.59%
61. 29%
78.68%
85.12%
88.48%
90.08%
92.01%
95.53%
94.14%
97.81%
99.86%
99.92%
99.95%
99.97%
0.00%
14 .11%
70.07%
69.41%
38. 71%
21. 32%
14.88%
11. 52%
9.92%
7.99%
4.47%
5.86%
2.19%
0.14%
0.08%
0.05%
0.03%
No Stripping Gas used in regenerator.
Component -------------------------------
STREAM REPORTS:
WET GAS STREAM
Temperature:
Pressure:
Flow Rate:
Water
Carbon Dioxide
Nitrogen
Methane
Ethane
Propane
Isobutane
n-Butane
Isopentane
n-Pentane
n-Hexane
Other Hexanes
Heptanes
Benzene
Toluene
Ethylbenzene
Xylenes
90.00 deg. F
414.70 psia
l.63e+005 scfh
Remaining Distilled
in Glycol Overhead ----------------------
29.49% 70.51%
0.00% 100.00%
0.00% 100.00%
0.00% 100.00%
0.00% 100.00%
0.00% 100.00%
0.00% 100.00%
0.00% 100.00%
0.55% 99.45%
0.54% 99.46%
0.52% 99.48%
1.06% 98.94%
0.51% 99.49%
5.01% 94.99%
7.91% 92.09%
10.41% 89.59%
12.92% 87.08%
Component Cone. Loading
(vol%) (lb/hr)
Page: 3
Water l.89e-001
Carbon Dioxide l.05e+000
Nitrogen 6.39e-001
Methane 8.58e+001
Ethane 6.04e+000
Propane 3.46e+000
Isobutane 8.68e-001
n-Butane 8.68e-001
Isopentane 4.19e-001
n-Pentane 4.19e-001
n-Hexane 5.99e-002
Other Hexanes 4.99e-002
Heptanes 8.98e-002
Benzene 9.98e-003
Toluene 9.98e-003
Ethylbenzene 9.98e-003
Xylenes 9.98e-003 ----------------------------------------
DRY GAS STREAM
Temperature:
Pressure:
Flow Rate:
Total Components
90.00 deg. F
414.70 psia
l.63e+005 sefh
100.00
Component Cone.
(vol%)
Water l.37e-002
Carbon Dioxide l.05e+000
Nitrogen 6.40e-001
Methane 8.60e+001
Ethane 6.05e+000
Propane 3.47e+000
Isobutane 8.69e-001
n-Butane 8.69e-001
Isopentane 4.19e-001
n-Pentane 4.19e-001
n-Hexane 5.98e-002
Other Hexanes 4.99e-002
Heptanes 8.94e-002
Benzene 8.82e-003
Toluene 8.20e-003
Ethylbenzene 7.30e-003
Xylenes 6.40e-003 ----------------------------------------Total Components 100.00
LEAN GLYCOL STREAM
Temperature: 90.00 deg. F
Flow Rate: 6.7le-001 gpm
Component Cone.
(wt%)
1. 46e+001
l.98e+002
7.68e+001
5.9le+003
7.79e+002
6.56e+002
2.17e+002
2.17e+002
l.30e+002
l.30e+002
2.22e+001
l.85e+001
3.86e+001
3.35e+000
3.95e+000
4.55e+000
4.55e+000 ---------
8.42e+003
Loading
(lb/hr)
l.06e+000
l.98e+002
7.68e+001
5.9le+003
7.79e+002
6.55e+002
2.16e+002
2.16e+002
l.30e+002
l.30e+002
2.2le+001
l.84e+001
3.84e+001
2.95e+000
3.23e+000
3.32e+000
2.9le+000 ---------8.40e+003
Loading
(lb/hr)
TEG 9.84e+001 3.7le+002
Water l.50e+000 5.67e+000
Carbon Dioxide 6.52e-012 2.46e-0ll
Page: 4
Nitrogen l.75e-013 6.59e-013
Methane 4.38e-018 l.65e-017
Ethane 2.92e-008 l.l0e-007
Propane 4.25e-009 l.60e-008
Isobutane l.SBe-009 5.98e-009
n-Butane l.77e-009 6.67e-009
Isopentane 2.4le-004 9. lle-004
n-Pentane 3.12e-004 l.lBe-003
n-Hexane 9.7le-005 3.67e-004
Other Hexanes l.2le-004 4.SBe-004
Heptanes 3.48e-004 l.3le-003
Benzene 5.Sle-003 2.0Be-002
Toluene l.62e-002 6. lle-002
Ethylbenzene 3.78e-002 l.43e-001
Xylenes 6.43e-002 2.43e-001
---------------------------------------- ---------
Total Components 100.00 3.78e+002
RICH GLYCOL STREAM
Temperature:
Pressure:
Flow Rate:
NOTE: Stream
90.00 deg. F
414.70 psia
7.12e-001 gpm
has more than one phase.
Component Cone. Loading
(wt%) (lb/hr)
TEG 9.34e+001 3.7le+002
Water 4.83e+000 l.92e+001
Carbon Dioxide 6.19e-002 2.46e-001
Nitrogen l.67e-003 6.62e-003
Methane l.24e-001 4.92e-001
Ethane 5.BBe-002 2.34e-001
Propane 9.92e-002 3.94e-001
Isobutane 5.0le-002 l.99e-001
n-Butane 6.76e-002 2.69e-001
Isopentane 4.SBe-002 l.82e-001
n-Pentane 5.93e-002 2.36e-001
n-Hexane l.84e-002 7.33e-002
Other Hexanes l.lSe-002 4.SBe-002
Heptanes 6.6le-002 2.63e-001
Benzene 1. ose-001 4.16e-001
Toluene l.95e-001 7.73e-001
Ethylbenzene 3.45e-001 l.37e+000
Xylenes 4.73e-001 l.BBe+000
Total Components 100.00 3.97e+002
FLASH TANK OFF GAS STREAM
Temperature:
Pressure:
Flow Rate:
105.00 deg. F
144.70 psia
l. l0e+00l sefh
Component Cone. Loading
(vol%) (lb/hr)
Water 9.12e-002 4.74e-004
Carbon Dioxide 2.73e+000 3.47e-002
Page: 5
Nitrogen
Methane
Ethane
Propane
Isobutane
n-Butane
Isopentane
n-Pentane
n-Hexane
Other Hexanes
Heptanes
Benzene
Toluene
Ethylbenzene
Xylenes
-------------------------------
Total Components
FLASH TANK GLYCOL STREAM
Temperature: 105.00 deg. F
Flow Rate: 7.l0e-001 gpm
Component
-------------------------------
TEG
Water
Carbon Dioxide
Nitrogen
Methane
Ethane
Propane
Isobutane
n-Butane
Isopentane
n-Pentane
n-Hexane
Other Hexanes
Heptanes
Benzene
Toluene
Ethylbenzene
Xylenes -------------------------------
Total Components
REGENERATOR OVERHEADS STREAM
Temperature:
Pressure:
Flow Rate:
212.00 deg. F
14.70 psia
3.17e+002 sefh
5.73e-001 4.64e-003
7.37e+001 3.42e-001
l.04e+001 9.0Se-002
6.59e+000 8.40e-002
l.77e+000 2.97e-002
l.84e+000 3.l0e-002
8.67e-001 l.Ble-002
9.03e-001 l.BBe-002
1. 32e-001 3.28e-003
1.0Be-001 2.69e-003
1. 99e-001 5.76e-003
2.52e-002 5.69e-004
2.39e-002 6.37e-004
2.04e-002 6.26e-004
l.Ble-002 5.57e-004
--------- ---------
100.00 6.68e-001
Cone. Loading
(wt%) (lb/hr)
--------- ---------
9.35e+001 3.7le+002
4.84e+000 l.92e+001
5.33e-002 2. lle-001
5.00e-004 l.98e-003
3.79e-002 l.Sle-001
3.6le-002 l.43e-001
7.82e-002 3.l0e-001
4.27e-002 l.70e-001
5.99e-002 2.38e-001
4.13e-002 l.64e-001
5.46e-002 2.17e-001
l.77e-002 7.00e-002
l.09e-002 4.3le-002
6.48e-002 2.57e-001
1. ose-001 4.15e-001
1. 95e-001 7.73e-001
3.45e-001 l.37e+000
4.74e-001 l.88e+000 --------- ---------
100.00 3.97e+002
Component Cone. Loading
(vol%) (lb/hr)
Water 9.02e+001 l.35e+001
Carbon Dioxide 5.76e-001 2.lle-001
Nitrogen 8.48e-003 l.98e-003
Methane l.12e+000 l.Sle-001
Page: 6
Page: 7
Ethane 5.7le-001 l.43e-001
Propane 8.43e-001 3.l0e-001
Isobutane 3.S0e-001 l.70e-001
n-Butane 4.9le-001 2.38e-001
Isopentane 2.7le-001 l.63e-001
n-Pentane 3.58e-001 2.16e-001
n-Hexane 9.69e-002 6.97e-002
Other Hexanes 5.93e-002 4.27e-002
Heptanes 3.06e-001 2.56e-001
Benzene 6.0Se-001 3.94e-001
Toluene 9.26e-001 7. lle-001
Ethylbenzene l.39e+000 1. 23e+000
Xylenes l.85e+000 l.64e+000 ---------------------------------------- ---------
Total Components 100.00 l.95e+001