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HomeMy WebLinkAbout1.0 Application Part 2March 2005 Noble Energy, lnc. Hyrup Production Facility Emissions lnventory Specific emissions factors are found in Table 2-4 "Oil and Gas Production Operations Average Emission Faclors." Estimate the number of equipment types for the maximum operating system to obtain maximum emissions estimates for permitting purposes. Applicable service areas include gas and light oil. Calculation method includes using the conservatively estimated number of equipment types, the emission factor (converted to lbs/hr/component), and the weight fraction of VOCs and HAPs in the streams. For consistency, use the gas chromatographic analysis for both the gas and light oil streams. Use equation in Section 2.4.6 to correct TOC factors to VOC factors: TOC = total gas components - CO2 - N2 = 96.643 wt % VOC = TOC - methane - ethane = i4.279 tt/t% Em (VOC)= Em (TOC)'wt%(VOC) / wt%(TOC) Em (VOC) = Em (TOC)' 14.279 / 96.643 Em (VOC) = Em OOC). 0.1477 Sample calculation: Gas service equipment E(TOC) = Em factor'M frac TOC 'number in service E(TOC) = Em factor (9.9E-3) lbihr/source'M frac TOC (.96643) ' number in service (60 sources) Emissions TOC = 0.574 lbs/hr TOC emissions from valves in gas service Emissions VOC = 0.670 ' 14.279 196.643 = 0.085 lbs/hr VOCs convert to TPY at 8760 hrs/yr = 0.37'l TPY VOC Light Oil service equipment E(TOC) = Em factor - wt frac TOC ' number in service note: assume liquid is 100% VOCs E(TOC) = Em factor (5.5E-3) lb/hrlsource 'M frac TOC (1.0) ' number in service (40 sources) Emissions TOC = 0.220 lbs/hr TOC emissions from valves in gas service Emissions VOC = TOC (light oil is 100% VOCs) 0.220 lbs/hr VOCs convert to TPY at 8760 hrs/yr = 0.964 TPY VOC Table 2-4 data. TOC TOC Number in TOC VOC VOC Equipment type Service Em. Factor Em. Factor Service Emissions Emissions Emissions kg/hrlsource lbs/hr/source (est) lbs/hr lbs/hr TPY Valves Gas 4.50E-03 9.90E-03 60 0.574 0.085 0.371 Light Oil 2.508-03 5.50E-03 40 0.220 0.220 0.964 Pump Seals Gas 2.40E-03 5.28E-03 0 0.000 0.000 0.000 Light Oil 1.30E-02 2.868-02 2 0.057 0.057 0.251 Others (1) Gas 8.80E-03 1.94E-02 10 0.187 0.028 0.121 Light Oil 7.50E-03 1.65E-02 5 0.083 0.083 0.361 Connectors Gas 2.00E-04 4.408-04 80 0.034 0.005 0.022 Light Oil 210E-04 4.62E-A4 50 0.023 0.023 0.101 Flanges Gas 3.90E-04 8.58E-04 30 0.025 0.004 0.016 Light Oil 1.10E-04 2.428-A4 20 0.005 0.005 0,021 Open-ended liner Gas 2.00E-03 4.40E-03 0 0.000 0.000 0.000 Light Oil 1.40E-03 3.08E-03 0 0.000 0.000 0.000TOTALSCnS:ffi TOTALS LIQUID: 0.388 0.388 1.698 TOTAL: 1.208 0.509 2.229 (1) Others = equipment types such as cornpressors, diaphragms, drains, dump arms, hatches, instruments, meters, PR valves, etc. Page 9 of 10Rinko, LLC Scan31 1. November 04. 2005.max Air Permit Support Documentation March 2005 Noble Energy, lnc. Hyrup Production Facility Emissions lnventory 7 Emissions lnventory - Detailed emissions calculations and supporting documentation for a Natural Gas compression station located in Garfield County, Colorado. Owner / Operator - Noble Energy, lnc., Houston, TX Site Name - Hyrup Natural Gas Production Facility Site Location - Garfield County, Colorado Overall Facility Overview List of Emission Sources 1,2 Two (2) Compressors 3 One (1) GtycolDehydration Untt 4 One (1) Reboiler Combustion Source for Glycol unit 5 Condensate Loading and Transportation 6 One (1) Condensate Storage Tank 7 Fugitive Emissions 8 Pigging Emissions 9 One (1) Process Water Storage Tank 10 One (1) Emergency Flare Facility Processing Rates Start-up processing rate is 1.5 MMSCFD supported by 3_5 wells Design processing rale is I MMSCFD supported by 12-1 5 wells Maximum configuration processing rate is 22 MMSCFD Condensate Production Rates Start-up processing rate to generate 5 bbl per day Design processing rate to generate S0 bbl per day Maximum processing rate to generate 1S0 bbl per day Abbreviations MM million SCFD standard cubic feet per day HP Horsepower bhp Brake Horsepower Hr Hours NOx Nitrogen oxides CO Carbon monoxide HCT Total hydrocarbons NMHC Non-methane hydrocarbons bbl Barrel, or 42 gallons Natural Gas Composition See attached for chromatographic analysis of representative sample, Hyrup No. 2-56. Summary of data appears below. Methane 88.?29% Mole yo Ethane 5.980% Mote % CO2 1.416% Mole % Hydrogen sulfide 0.00070 Mole % Heating Value 1,134 BTU/SCF dry basis Condensate 'l .22 gal / 1000 SCF Page 1 of 10Rinko, LLC Scan303, November 04. 2005.max Air Permit Support Documentation March 2005 Noble Energy, lnc. Hyrup Production Facility Emissions lnventory HAP emissions Use the gas chromatographic analysis for weight percent HAP species to estimate HAp emissions,keeping the overall weight percents for gas and the oil weight percenls for liquids. GAS VOC annual emission = n-Hexane Benzene 2,2,4-Trimethytpentane Toluene Ethylbenzene Xylenes Acetaldehyde Acrolein Formaldehyde Methanol Totals Pigging Emissions 0.458 0.048 0.0 0.257 0.024 0.240 0.0 0.0 0.0 0.0 0.002 0.000 0.0 0.001 0.000 0.001 0.0 0.0 0.0 0.0 4 0.51 0.0 2.73 0.25 2 0.531 TPY HAP Emissions lO VOC =1.698 TPY HAP Emissions 0.122 244 0.0 0.0 0.0 0.0 HAP Totals 0.128 2s5J 3 0.057 113.780.006 11.920.0 0.00.032 63.850.003 5.960.030 59.620.0 0.00.0 0.00.0 0.00.0 0.0 Assume fuil-scale system will include a pigging receiver and site will incur pigging losses which willresult in blowdown and evaporative losses. Equipment detail not available at this time. For a conservativeestimate, use approximately 1 ton per year total Voc emissions as a working estimate. Assurne the pigging operations will occur once per week over one shift, or g hrsA,vk'S2 wks/day = 416 hrslyrUse M% for liquid (condensate) to represent emissions. VOC emissions:1.00 TPYVOCs 4.81 lbs/hr VOC HAP Emissions . HRP wtY,-tiqEn-Hexane 3.208 0.032 --- 64Js Benzene 2,2,4-Trimethylpentane Toluene Ethylbenzene Xylenes Acetaldehyde Acrolein Formaldehyde Methanol Totals Emergency Flare 0.336 0.0034 0.0 0.01.800 0.0180.168 0.00171.681 0.a17 0.0 0.0 0.0 0.0 0.0 0.0 6.72 0.0 36.00 3.36 33.62 0.0 0.0 One emergency flare to be located-at the site. from this source. 0.0 0.0 0.0 0.00.072 143.848 Flare functions only during upset condilions. Negligible emissions Page 10 of 10 3.208 0.054 .t 08.920.336 0.006 11.420.0 0.0 0.1.800 0.031 61.120.168 0.003 5.711.681 0.029 57.080.0 0.0 0.0.0 0.0 0.00.0 0.0 0.00.0 0.0 o Rinko, LLC Scan312, November 04, 2005.max Air Permit Support Documentation HAP 'ttto/o oo APPBNDIX 6 SOURCE DATA and MODELING RUN PRINTOUTS HYR{JP PRODUCTION FACTLITY NOBLE trNERGY INC. GARIIELD COUNTY, COLORADO Scan313, November 04, 2005.max FESCO, Ltd. 1100 Fesco Ave. - Alice, Texas 78332 For: Noble Energy, lnc. '100 Glenborough, Suite 100 Houston, Texas 77067 Sample: Hyrup No. 2-56 Spot Gas Sample Date Sampled: 12-06-04 December 13,2004 Job Number: 45573.001 1.591 0.528 0.125 0.138 0.006 0.061 0.059 0.095 0.410 3.013 Certified:FESCO, Ltd,Alice, Texas CHROMATOGMPH EXTENDED ANALYSIS . SUMMATION REPORT COMPONENT MOL% GPM Nitrogen 0.097 Carbon Dioxide 1.416 Methane 88.229 Ethane 5.980 Propane 1.925 lsobutane 0.384 n-Butane 0.441 2-2 Dimethylpropane 0.016 lsopentane 0.168 n-Pentane 0.165 Hexanes 0.231 Heptanes Plus 0.948 Totals 100.000 Computed Real Characteristics Of Heptanes Plus: Specific Gravity 3.607 (Air=1) Molecular Weight 104.17 Gross Heating Value 5404 BTU/CF Computed Real Characteristics Of Total Sample: Specific Gravity 0.671 (Air=1) Compressibility (Z) ---- 0.9971 Molecular Weight 19.37 Gross Heating Value Dry Basis 1149 BTU/CF Saturated Basis ------ 1'130 BTU/CF Base Conditions: 14.650 PSI & 60 Deg F Analyst: JG Processor: LS Pagel ot2 Scan314, November 04. 2005 max David Dannhaus 361-661-7015 FESCO, Ltd.Job Number: 45573.001 CHROMATOGRAPH EXTENDED ANALYSIS TOTAL REPORT MOL% GPMCOMPONENT Nitrogen Carbon Dioxide Methane Ethane Propane lsobutane n-Butane 2,2 Dimethylpropane lsopentane n-Pentane 2,2 Dimethylbutane Cyclopentane 2,3 Dimethylbutane 2 Methylpentane 3 Methylpentane n-Hexane Methylcyclopentane Benzene Cyclohexane 2-Methylhexane 3-Methylhexane 2,2,4 T rimelhylpenta ne Other C7's n-Heptane Methylcyclohexane Toluene Other C8's n-Octane Ethylbenzene M & P Xylenes O-Xylene Other C9's n-Nonane Other C10's n-Decane Undecanes Plus Totals 0.097 1.416 88.229 5.980 1.925 0.384 0.441 0.016 0.168 0.'t65 0.006 0.008 0.013 0.066 0.035 0.103 0.045 0,012 0.060 0.029 0.028 0.000 0.062 0.092 0.1 76 0.054 0.161 0.055 0.004 0.039 0.005 4.074 0.019 0.024 0.003 0.005 100.000 1.591 0.528 0.125 0.1 38 0.006 0.061 0.059 0.002 0.003 0.005 0.027 0.014 0.042 0.015 0.003 0.020 0.0'14 0.013 0.000 0.027 0.042 0.070 0.018 0.074 0.028 0.002 0.015 0.002 0.038 0.010 0.014 0.002 0.003 3.013 wT% 0.140 3.217 73.080 9.284 4.383 1.152 1.323 0.060 0.626 0.6't s 0.027 0.029 0.058 0.295 0.1 56 0.458 0.195 0.048 0.259 0.151 0.1 45 0.000 0.318 0.477 0.89.1 0.257 0.917 0.327 0.024 0.211 0.029 0.484 0.124 0.178 0.023 0.039 100.000 Computed Real Characteristics of Total Sample Specific Gravity --*- Gross Heating Value Dry Basis --- Saturated Basis ------- Page 2 of 2 Compressibility (Z) Molecular Weight 19.37 0.67'l (Air=1) 0.9971 1149 BTU/CF 1130 BTU/CF Scan315, November 04, 2005 max (o.o, tOt $s ON mot4tuqfoFo 3rNoloHlrol- ll U.'3,,d f,(,T= =E o TJJFL coalo_0+-5 )JfFtl 'F H Yu)o- ru></) a vJtr, L! rt f c) E I I* rp=soock rL r FO0() t q=H H.c)3<f) la o-t- @F- NO$ OOO F60 Orh n \iltr ooro @ lo@o @rnF- r loOe C)O() s lra': '. c; q q l.\oo o o o l- OOrO6(O(OOOOOFOoO Noq s$o N N t6OO NF$ N O, O I N- +9c? 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TEG Dehydratj-on Unit (Natco) of Operation:8760.0 hours,/yr EMTSSIONS REPORTS: CONTROLLED REGENERATOR EMTSSIONS Component Ibs,/hr 1bs ,/da y tons,/yr Methane E thane Propane I sobutane n-Butane Isopentane n-Pentane Cyc].opentane n-Hexane Cyc.].ohexane Other Hexanes Heptanes Met.hy lcyclohexane Benzene To luene Et hylbenzene Xylenes CB + Heavi-es 6.1133 2 .1951 1.5340 0.4986 o -1096 o .267 2 0.3433 0.0537 o - 2386 o.4803 o .3497 0.5001 1.0156 o .5926 7.'1 861 o.o72B 0. 9606 0.0r-95 146.720 52 .698 36.816 1L.966 1-7.030 6-412 B -239 1_-289 5-726 41.526 8.393 t2 . oo2 24 .391 1A aaaL1 . ZLZ 42 . AB2 7 -7 4'7 23. O53 o.469 26.1'7 64 9 .6113 6.1789 2.7A37 3- 1-079 1, . 1,7 02 1. s036 o .2352 )..o449 2 . L035 1.5318 2.1,904 4.4525 2 . s954 7 .8259 o.31BB 4 .20'7 2 o.o856 Total TotaI Hydrocarbon Total_ VOC TOtA} HAP Total BTEX Emissions Emissi-ons Emissions Emissions Emi s s ions t'7 .7 321 !1 .'? 327 9 .4237 3.65L2 3 - 4L21 425.586 425.586 226. L68 87 .629 81.904 77.6694 77 .6694 4L.2751 1,5 .9923 t4-9414 UNCONTROLLED REGENERATOR EMTSSTONS Component Scan320, November 04, 2005.max lbs /hr 1bs,/day tons,/yr Methane E t.hane Propane f sobutane n-Butane 6 .727 I 2 .2215 t . 62'11 0.5592 0.8260 147. O51 53.317 39. O6s )_3 . 422 t9 .823 26 .8369 9.7303 7 .1294 2.4495 3 .6711 Isopentane n- Pen t ane Cyclopenta ne n-Hexane Cyc I ohexane Other Hexanes Hept a ne s Methy l- cyc l ohexane Ben z ene ToLuene Ethy-l- ben z ene XyJ-enes CB+ Heavies o.3820 o - 5131 o.o94B o .5402 r-.3363 o .67 66 2.1953 4.1378 1.9224 13.9795 1.491_O 22 .267 622.3989 9.168 ).2 - 314 2.276 1,2 .964 32.O72 1_6.238 52 .681 113.706 46.1"36 335.509 35.783 534.423 537.575 Page: 2 1,.6732 2 .247 4 o-4154 2 .3660 5.8532 2.9634 9.6154 20 .'7 5t4 8.4199 61, .2303 6.5304 9'l .5323 9B.tO74 Total Hydrocarbon TotaI VOC Total HAP TOIA1 BTEX ToLaJ- Emi-ssions Emissions Emi s s ions Emi-ssions Emissions 83.8971 83.8971 75-5485 40.2007 39.660s 2013-531 2013.531 1813.163 964 .81,6 95L .8s2 367 .4694 361 .4694 330 .9022 L16.0189 173.7130 COMBINED REGENERATOR VENT,/FLASH GAS EMISSTONS Component 1bs,/hr 1bs,/ctay tons /yr Me thane Ethane Propane f sobutane n - Butane f s opentane n- Pentane Cyclopent ane n -Hexa ne Cyc I ohexane Other Hexanes Hept,anes Me th y1 cyc 1 ohexane Benzene To Iuene Et hy1 ben zene X ylenes CB+ Heavies 6.1_133 2.1957 1.5340 o.4986 o.7096 0.2672 0.3433 o. 0537 o-2386 o.4803 o - 3497 0.5001 1. O166 o.5926 1.1867 o.o't28 0.9606 o.0195 L46.120 52 .698 36-816 11.966 17 - 030 6.41_28.239 1.289 5.726 L1 - 526 8.393 72 . OO2 24.391 14 .222 42 .882 ].-747 23. O53 o.469 26.77 64 9.6L73 6 .7-t 89 2 .783'7 3.1079 1, .17 02 1.5036 o .2352 7-O449 2. 1-O3s 1.5318 2.1,904 4 .4525 2.59s4 7.8259 0.3188 4.2012 0.08s6 TotaI Emissions TotaI Hydrocarbon Emissions Totaf VOC Emissions Tota.I HAP Emissions TotaI BTEX Emissions 11 .'t 32'7 l-t .1 321 9.423'7 3 .6s72 3.4\2-t 425 .586 425.546 226.168 8'7 .629 81.904 't1 .6694 7'7 . 669 4 4L.2'75'7 L5 .9923 14.9474 COMBINED REGENERATOR VENT/FLASH GAS EMISSION CONTROL REPORT: Uncontrolled tons,/ yr Controlled tons,/yr Component Scan321, November 04, 2005.max * Reduction Metha ne Ethane Propane I sobutane n-But.ane fsopentane n-Pentane Cyclopentane n-Hexane Cyc lolrexane Other Hexanes Heptanes Methy 1 cyc lohexan e Ben zene To luene Et hyJ-ben zene XyIene s CB+ Heavies 26 .8369 9.7303 7.1294 2.4495 3 . 6L1-7 L.6'732 2.2474 o.4154 2 .3660 5.8532 2 .9634 9.6154 20.7514 8.4199 6'l_ .2303 6.5304 97 .5323 98 -LO7 4 26.7764 9 .6t1 3 6 .1 1A9 2 . tB37 3.1079 1.1'7A2 1. s036 o .2352 7.O449 2.1035 1.5318 2 .1904 4 .4525 2.5954 '7 - 8259 0.3188 4 .2072 0.0856 Page: 3 o.23 1.16 5.7 6 10.85 14.O9 30. o6 33.10 43.38 55.84 64.06 48.31 7't .22 78.54 69.t1 81 .22 95.t2 95, 69 99.91 Tota 1 TotaI Hydrocarbon Tota l- VOC Total- HAP Total BTEX Emissions Emissi-ons Emissions Emi s s ions Eml s s ions 36-t .4694 367 .4694 330 .9022 L'76.0789 L1 3 .7 130 '7 1 .6694 '77 - 6694 47.21 5'7 t5 .9923 L4 .947 4 78. B6 78. B6 87.53 90 .92 91.40 EQUIPMENT REPORTS: CONDENSER Condenser Outlet Temperature: Condenser Pressure: Condenser Duty: Hydrocarbon Recovery: Produced Water: VOC Control Efficiency: HAP Contro]- Efficiency: BTEX ControL Effici_ency: Dissolved Hydrocarbons in Water: Compone n t 115.O0 12 .50 6. OZe-OO2 5.33 4.7"t 87.53 90-92 91.40 333.39 Emitted deg. F psia MM B'I'U,/hr bbI s,/day bbls,/day 6t I mq/t- Condensed Water Carbon Dioxide N i t rogen Methane Ethane Propane T sobutane n-But ane I sopentane n- Pentane Cyclopenta ne n-Hexane Cycl ohexane Other Hexanes 2 ,232 99 .25* 99 .'7 6\ 99.77* 98.84* 94 .24* 89.15r 85.91E 69 .94?^ 66 .90* 56.622 44.L6* 3s.94r 51.698 9't -772 0.758 o-242 0.23t 1.16t 5-16* 10.85s 14.09? 30. o6r 33. 108 43.38r 55.848 64 . O6z48.31t Scan322, November 04, 2005.max Hept anes Me t hy 1 cyc lohex ane Be n zene To I uene Ethy lben zene Xyl enes C8+ Heavies 22.78* 21,.46* so.B3g't2.78Z 4.88t4.31t 0.09t Page '7 7 .22* 1 B .54* 69-L7* 87 -22* 95 . L2* 95.69* 99.91,* ABSORBER NOTE: Because the CalcuLated Absorber Stages was below the minimuma11owed, GRr-cl,Ycalc has set the number of Absorber stages to L.25and has calculated a revised Dry Gas Dew point. Calculated Absorber Stages: 1.25Cal.cuJ-ated Dry Gas Dew point: 6.49 Temperature: 1 1O. OPressure: 900. ODry Gas Fl-ow Rate: 22. OOOOGlycol Losses with Dry Gas: 0.5246Wet Gas Water Content: SaturatedCalculated liet Gas Water Content: 83,91Speci fied Lean GJ.ycol Recirc. Ratio: 3 . OO Component Rema ini ng in Dry Gas Lbs. H2O,/MMSCF deg. F ps ig MMSCF,/da y 1b,/ h r Ibs. H2O,/MMSCF qal/lb H2o Absorbed in GlycoJ. I'la te r Carbon Dioxide N j. t rogen Metha ne Ethane Propane Isobutane n-But ane I sopen tane n- Pen t ane Cyclopent ane n-Hexane Cycl ohexane Other Hexanes Hept anes Me t hyI cycl ohexane Ben zene To1 uene Ethylben zene XyI ene s CB+ Heavies 1 .7't_* 99.80t 99.98E 99. 9Br 99. 958 99 .92* 99.908 99.87t 99.87r 99.848 99.30t 99.75* 98.918 99.80? 99. s78 98.878 9t - 52* 88.38? B5.4Bt B0.2Br 98.40* 92 - 29* o .20sb, o.o2Z o.o2*0.05t 0. oBt 0.10t 0.13* 0.13* 0-16t o.708 0 .25* 1. O9t 0.208 0.438 1.138 B.4BT L7 .622 t4 .522 t9 .7 2Z r-.60t REGENERATOR No Stripping Gas used in regenerator Scan323, November 04, 2005.max Component Remaining in GIycol page Dist.i]-Led Ove rhead WaterCarbon Dioxide Ni t rogen Methane Ethane propane I sobutane n -ButaneIsopentane n- Pen t ane Cyclopentane n-Hexane Cyc lohexane Other Hexanes Hepta ne s Methyl cyc I ohexane Ben zene Toluene Ethylben zene XyI enes CB+ Heavies 29 - 40? o. oo8 o. o0r o. o08 o.008 0. o0? 0. oot 0. 00t0.50t 0.50r 0.50a o. sos 3 .20* 1. 00t o.508 4. OO* 5.00E 7 .902 10.40* L2.90* 72 . OOZ 70.60a 100. ootr-o0.00t100.oot 100.oo8 100.008 100.00t 100. oot 99. so? 99.508 99.503 99.508 96.80ts 99.008 99.s03 96.00* 95.00r 92.10t 89.608 B?.103 88.00ts STREAM REPORTS: WET GAS STREAM Temperature: Pressure: Flow Rate: L1O. OO deg. E. 914 -7 O psia 9. 1 9e+OO5 scfh Component Conc. (vol-t)Load i ng ( Ib,/hr) Water Carbon Dioxide N i t rogen Me ehane Ethane Propane I sobutane n-Bu tane I sopentane n- pent ane Cycl opentane n-Hexane Cycl ohexane Other Hexanes Heptanes Me t hyI cyc I ohexane Ben zene Tol uene 1 . 7 7e-O01- 1. 4 1e+000 9. 68e-002 B . B 1e+OO1 5 - 97e+000 1.92e+000 3.83e-0O1 4 . 4 Oe-001 1.68e-001 1.81e-001 7.99e-003 1.03e-O01 5. 99e-002 1 . 65e-OO 1 2 - 11e-OO1 7.71e+OO1 1.51e+0O3 6.57e+0O1 3 .42e+OO4 4 .35e+003 2. O5e+003 5.39e+O02 6 .2Oe+O02 2 .93e+OO2 3. 1- 6e+002 1.36e+0O1 2 .'1,5e+OO2 7 .22e+OO2 3.44e+OO2 5. 1 1e+002 1.76e-OO1 4.18e+OO2 1.20e-OO2 2-27e+OO7 5.39e-O02 !-2Oe+OOZ Scan324, November 04, 2005.max Page:Ethylbenzene 3.99e-003 Xylenes 4.39e-O02 1.03e+001 1.13e+OO2 CB+ Heavies 3.40e-O01 1.4Oe+OO3 Total Components 1OO. OO 4.73e+OO4 DRY GAS STREAM Temperature: Pres sure : Flow Rate: 110.OO 97-4.-lO 9. 17e+O05 Component deg. F psia scfh Conc. (voI8) Loading ( 1blhr) Water Carbon Dioxide Ni t rogen Me thane Ethane Propane I sobu tane n-Butane Isopentane n - Pent ane Cycl open t ane n -HexaneCyclohexane Other Hexanes Hept ane s Methyl cycJ-ohexane Ben zene To 1 uene E t hy Iben zene Xylenes 1. 37e-002 5. 95e+O0O 1 . 4 1e+O0O 1. 5Oe+OO3 9.7Oe-OO2 6.57e+OO1 B. B2e+001 3. 42e+O04 5.98e+0O0 4.34e+OO3 1.92e+000 2. O5e+OO3 3. B4e-OO1 5. 39e+002 4.41e-001 6.19e+O02 1 . 6Be-OO1 2.93e+OO2 1. B1e-OO1 3.15e+0O2 7.95e-O03 1.35e+0O1 1. O3e-001 2.74e.+OO2 5. 94e-OO2 1.27e+OO2 1.65e-O0l- 3.43e+002 2.1Oe-001- 5.09e+002 1.74e-OO1 4.13e+OO2 1.10e-002 2.07e+0O1 A.'7 1e-OO2 1. O6e+0O2 3.42e-O03 8.77e+0O0 3.53e-O02 9.06e+0Ol- CB+ Heavies 3.36e-001 1.38e+0O3 TotaI Components 100.0O 4.'72e+OO4 LEAN GLYCOL STREAM Tempera tu re : Fl-ow Ra te : 110.OO 3.51e+OOO Component deg gpm Conc. (wtt) Loading ( 1blhr ) TEG Water Carbon Dioxide Ni t rogen Me t hane Etha ne Propane I sobut ane n-Butane f sopentane 9.81e+O01, 1.94e+OO3 1.50e+0O0 2.96e+OO1 1.52e-011 3. O1e-01-O 6.63e-014 1.31e-O12 1.04e-017 2.06e-016 5.31e-008 1.05e-006 3.36e-009 6.62e-OOa B.5Oe-O1O 1.68e-OO8 1.04e-O09 2.05e-0OB 9.73e-OO5 1.92e-0O3 Scan325, November 04, 2005.max Page: n- Pentane Cyc I opentane n-Hexane Cy c1 ohexane Other Hexanes H ept ane s Me th y l cyc J- ohe xane Ben zene Tol uene EthyJ-ben zene Xylenes cB+ Heavies 3Le-O04 2 - 5Be-OO3 42e-O05 4.7 7e-O04 38e-OO4 2.71e-0O3 24e-OO3 4.42e-OO2 4 6e-004 6. B3e-003 59e-004 1 - 1Oe-002 00e-002 1.9?e-OO1 13e-003 1. O1e-OOl- OBe-002 1.20e+OO077e-O03 1.73e-OO1 67e-O01 3.3Oe+000 55e-O01 3. O5e+0O0 L- 1. a ? q L. 6. 8. 1. 1. TotaI Components 100.0O 1.97e+003 RICH GLYCOL STREAM Temperature: Pressure: FIow Rate: NOTE: St ream 11O. 0o deg. F 914.1 O psia 3. B4e+OOO qpm has more than one Component pha se . Conc.(wtt ) Load i ng ( 1blhr ) TEG Water Carbon Dioxide N i t rogen Me t hane Ethane Propane I sobutane n-Butane I sopentane n - Pentane Cyclopentane n-Hexa ne Cyc Iohexane Other Hexanes Heptanes Me t hyl cycl- ohexane Benzene To J. ue ne Ethylben zene Xy Iene s CB+ Heawies 9.08e+O01 1. 93e+0O3 4.73e+000 1. O1e+0O2 1 . 4 1e-001 3. O1e+0OO 6. 16e-004 1. 31e-0O2 2. BBe-0O1 6.13e+0O0 l- - 04e-0O1 2.22e+OOO 1.64e-OO2 1-63e+000 2.63e-O02 5.59e-001 3.88e-OO2 8.26e-OO1 1. B0e-OO2 3.84e-001 2.42e-OO2 5. 16e-001 4.48e-0O3 9.53e-OO2 2 .55e-OO2 5. 4 3e-001 6.48e-OO2 1.38e+O00 3.21,e-OO2 6.83e-OO1 1.04e-OO1 2.21e+O0O 2 .32e*OOl 4 . 94 e+000 9.50e-0O2 2.02e+0OO 7.13e-001 1.52e+001 7.81e-0O2 1.66e+OO0 1.20e+0OO 2.56e+001 1.2Oe+000 2,55e+O0l- Tota]. Components REGENERATOR OVERHEADS STREAM 1O0. O0 2. 13e+003 Temperature; Pressure: Flow Rate: 2L2.OO deg. r 14.7O psia 1.97e+0O3 scfh Scan326, November 04, 2005,max Page:Component Conc. (voI8)Loading ( 1blhr ) Wacer Carbon Dioxide Nitroqen Methane Et hane propane T sobutane n -Bu t ane I sopentane n- pen tane Cyc I openta ne n -Hexane Cyc 1 ohexa neOther Hexanes Heptanes Me thy I cyc Iohexane Ben zene To1 ueneEthyl-ben zene Xy]. enes C8+ tls6y1gg 7. L. o 7. 1. 7. t. 2. 1. 1. 2. 1. ? 1. 4. 62e+001 32e+OOO O3e-O03 37e+OOO 4 3e+O0O 12e-OOL B6e-O01 74e-O01 02e-O01 37e-00 1 7.11e+OO1 3. O1e+OOO 1.31e-OO2 6. L3e+OOO 2.22e+OOO 1.63e+OOO 5.59e-0O1 8.26e-OO1 3. B2e-OO1 5.13e-OO1 61e-002 9.48e-002 21e-O01 5-40e-0O1 O6e-O01 1.34e+OOO52e-O01 5.77e-0O123e-O01 2.2Oe+OOO 9.31e-001 4.75e-001 2.93e+000 2 .71-e-OOl 4. O5e+O0O 2.54e+O0O 4.74e+0OO 1 - 92e+0O0 1.40e+0O1 1 .4 9e+OOO 2 . 23e+OO 1 2 .24e+OOt Total Components CONDENSER VENT GAS STREAM 100.00 1.58e+002 Tempera t.ure :Pressure: Fl-ow Ra te : 115.00 12.50 2.81e+OO2 Compone n t deg. F psia scfh Conc. (volt) Load i ng ( 1b,/hr ) Wat erCarbon Di_oxide N i t rogen Methane Et hane propane I sobutane n-But a ne fsopentane n- pen ta ne Cyc I opent ane n-Hexane Cyclohexane Other Hexanes Hept a ne s Met hyI cyclohexa ne Ben ze ne To luene Et hylben zene Xylenes CB+ gs6r1." 1 . 1 9e+001 9.17e+00O 6.31e-OO2 5. 15e+001 9.8?e+O0O 4.70e+000 1.16e+000 1.65e+OOO 5. O1e-OO1 6. 4 3e-OO1 O3e-OO1 5. 1 Ae-OOL 2. 71e-001 4. 4Be-0O1 3.74e-001 5. 5Be+OOO 99e+00O 31e-OO2 11e+O0O 2Oe+OOO 53e+O0O 99e-O01 10e-OO1 67e-O01 43e-O01 37 e-OO2 39e-001 B0e-001 50e-O01 O0e-O01 t. z- 1. 6.) 1. 4. 7. a 1. 2 7. J- 6. 1. 1.) q 1. 1. 4 0e+000 O3e+000 62e+OOO 2-l e-OO2 22e+OOO 55e-OO2 1.02e+O0O 5. 93e-O0 1 1 . 7 9e+OOO '7 .28e-OO2 9. 61e-OO 1 1.95e-OO2 Scan327, November 04, 2005.max Total Components CONDENSER PRODUCED WATER STREAM 100. OO 2.23e+OO1 Temperat.ure: Flow Rate: 115.0O deg. F 1.39e-001 gpm Component Conc. (wtt ) Loading ( f b,/hr )(ppm) Water Carbon Dioxide Ni t rogen Methane Et'hane propane f sobutane n -Bu tane I sopen tane n - Pentane Cyclopen ta ne n -HexaneCyclohexane Other Hexanes Heptane s Me thyl cycl ohexane Ben zene Toluene E Ehylben zene Xylene s CB+ Heavj_es 1.00e+002 7. LBe-O03 7 .9te-OO't 7.22e-OO4 3. OOe-004 2. OBe-O04 3 . ? 1e-O05 7.04e-0O5 1 . B 9e-005 2.61e-005 2.93e-0O5 1 .52e-005 1,-16e-OO4 1.79e-005 l-.79e-0O5 1 . 7 9e-0O4 6.28e-003 l".5Be-002 4.88e-004 8.99e-003 4 .44e-OO7 6. 95e+00 1 5. OOe-OO3 5.50e-0O7 5. O3e-0O4 2. OBe-OO4 1 . 4 5e-OO4 2.58e-005 4 - 90e-0O5 1.31e-OO5 L. B2e-0O5 2.04e-0O5 1.06e-005 L.23e-OO4 1.25e-0O5 1.24e-0O5 L.24e-OO4 4.37e-OO3 1.10e-OO2 3 . 4 Oe-004 6.26e-003 3.09e-0O7 999595 -72 o 3 2. 0. 1. o. o. o. o. 2. o. o. 2. 63. 158. 5. 90. o. Tota.l_ Components CONDENSER RECOVERED OIL STREAM 1OO. OO 6. 96e+OO1 1000000 Tempe ra t u re :Flow Rate:115.00 deg 1.56e-OO1 gpm Component Conc. (wtt)Loading ( Ib,zhr) Water Carbon Dioxide Nitrogen Me tha ne E thane Propane I sobutane n-Butane fsopentane n-Pentane Cyclopen tane n-Hexane Cyclohexa ne Other Hexanes 3.59e-OO2 2 .66e-O02 4.71e-OO5 2 . Ole-OOZ 3. B7e-0O2 2 .3Be-OO2 7 .1 6e-OO2 3.16e-OO5 1.33e-OO2 2 .56e-OO2 L . 4 1e-0O1 9. 36e-0O2 9 . 1 6e-0O2 6. O6e-OO21.76e-OO1 1.l-6e-OO1 1.73e-001 1. 15e-001 2.57e-00L l.'70e-001 6.21e-OO2 4.11e-002 4.56e-OO1 3.02e-O011.29e+0O0 B.56e-O014.94e-OO1 3.27e-OO1 Scan328, November 04. 2005.max Page: Page: 1 0Heptanes 2.56e+OO0 1,70e+OOO Me t hy1 cyc J-ohexane Benzene To.].uene Ethylben zene Xy1 ene s C8+ Heavies 5. 62e+OOO 3.72e+OOO 2.0Oe+0OO 1-.33e+OOOl-.84e+OO1 L.22e+OOL2.14e+OO0 1.42e+O0O3.22e+OOL 2.13e+OO1 3.38e+001 2.24e+OOt TotaI Components CONDENSER CONTROL CURVE DATA REPORT: 10O. OO 6.62e+OO1 CONDENSER CONTROL EFr'ICIENCY CURVES Note: Condenser curves computed for the rangeDO NOT EXTRAPOLATE BEYOND THTS RANGE I 4O.O F <: T <: VOC 95 .92 95.65 95.36 95.05 94.77 94 .34 93. 93 93 .49 92 .99 92.45 91.85 91.18 90.44 89.61 88.67 B'7 .62 46.43 85.08 83.54 BJ. .7 7 19 -73 77.L9 14 .35'to.98 66.92 61.95 56.O1 170.0 F. Temp ( F) 40.o 45.O 50. o 55.0 60. o 6s. o 70. o 75 - O BO. O 85 - O 90.0 95. O l-oo. o l-05. o 110. O 115.0 120.0 125.0 130. O 135. O 140.O 145. O 150-O 155.0 160. O 165. O 170.0 BTEX 99 .22 99.01 98.90 98.69 94.45 98.18 9'7.86 9'7 .49 91 .06 96.5'7 96-O0 95.34 94 .58 93.70 92-68 91.50 90. 11 88.49 86.s9 84.34 81.68 78.26't4-33 69 .54 63. 68 56 - 46 47 -99 Total HAP 99.13 98.96 98.77 98.55 98 .29 91 .99 9'7 - 65 9'7 .2 6 96-BO 96.28 9s. 68 95. OO 94-2L 93 .29 92.24 97.O2 B9-51 87.96 86.O2 83.75 81.07't't .63 73.69 58.91 63. O7 55.89 47 - 49 ANNUAL AIR-COOLED CONDENSER PERFORMANCE: ANNUAL AIR_COOLED CONDENSER PERFORMANCE Nearest Site for Air Temperature Data: Ambient Air Dry Bulb Grand Junction, CO Scan329, November 04, 2005.max Page:Condenser Out. letTemperature (deg. F) 11Temperature (deg. F) <:5 O 51_55 56_60 61-65 66-1 A 7L_75 76-80 B1-85 B6-90 91-95 96-100 >100 Condenser outlet Frequency (* )4't .1,O 7,09 7 .2A 7 .82 7 .95 6.92 5.50 4 .21 3.39 2. t9o.60 0. o3 temperature approach <:7 0 71__7 5 7 6_80 B1_85 86-90 91-9s 96-100 101- 10 5 106-110 111-115 116-120 >120 to ambient: 20. OO deg AnnuaL air-coored condenser emissions and control efficiency: Benzene BTEX Tota-]. HAP VOC Uncont rol l- ed emi s s ions ton s,/ yea r B .420 L'7 3 - 71,3 1_76.O79 330 .902 Control].ed emissions ton s /yea r I .241, 5.852 6.406 24.41,2 t Contro.l- Bs .26 96.63 96.36 92 .62 o Scan330, November 04, 2005.max oo)(! o- YOCE66 !ooo 30-o>ocx5 E33pEOot>d .gao- r.* c? N ll 0) lo (!) (L .o oco-oo E O) oE(6 ooo oo a *, "9(!(Jtr([ ^=o:6 ^$.9;g E I 9tf ; = 6,P, Efl& h €FO)?,.e, L.9H ErO O xEolE o fi>'=E P #€.E q 5 eE'€ ,E*E$r( EE3Etc(s .> -IEE9EF E FT€EEE? cFf€tg{ qesEq{qgt '-r-o o o';ry s.,,..,o,r(oo3: aE:;;3E P.Pg E EES.EIIHEEEr F I * *TEETEOECHE T. E g PtoEEoooriE >!>Dio6if'ddrs;5a{g z 3.Bg6 io'aoc)-tf,co.") rro EOr oo (,ro 90 u;c .o 6 :,ooE5()oo .o6 .o E IU E o Y? ? roooN h.- (, : A ...::..s9 ie Ri,; ;i er E eEB q Ee eFa ;i Efi.t= :d B .#6e * eF;rsEHc= EsEss i # :Et s ;sEe:;S+f ;#*Ep ;Sss Ess g coE(g --OYeE c= oc lio'.: o E' E6 -o 6;.9 E;*gERH = o.t.lJ o io)bfo(/)oF.oE Scan331, November 04, 2005.max sa q) O) Go.l .9o:Fq o ilG o 8 ^i q 'd o sE 3'.9 33 'a Ed o Cto th9 aqfi 5o_6 ,o.OE F = o)I ? 0ooNt- 11 c t o Scan332, November 04.2005 max YOCD66 Looo &o.o.)ocxl E-3$r =o6E>3 g iE ,YtrtrF.E 6FtLO -tr)'is oE8{u(, Ay o ZY iE F<#E e3 5 <-r'6! o'=trE UJJ q c.) o(,)(! o- !oc!GGFb oooot_ o.4rC E3o--o:EO OE>6(9 G :6rfiT -o-,E< oPs,+? 5tD y'5jYX(!Z;E<ooFdEo(J o'a @a,,9o E u.t hpss: P8B8RB ffssE EE EBfi ulEE i qSgE E g HgEHff 5 E$qiSgg tBg383 -o-- oo o@odiliooo oiriri*dici o-or -i;-* 3.oo o o@No o ! @Now6 o o63.3 3_ 6 _.Hii ;__ fr _i.,_ *il;*;r+-- pa- n3=::aaa s itri sisrri' SFFFF iffffigffis grffiiiffffffiggisr g oooo $;i i ! Scan333, November 04, 2005.max $ ot(E& IOcrooo ooOOtY- orcxf;:o 3= =oOE>3 ao (g= L.- oxtrd =-([l ^ brN'ioYs rO-9rS2Ls<0rlF(r.YvO(E .ed 3 ,,1 lUo oo o9 000@oNooo @No oo tso@ooo voo oo ooEooo vqq q?o qqqoqo qr@ OO mOvOor r@@ O o @rr rjELJ 6-r = O! Y? c? 6ooa{ l- o p 5 9rl90lFoS + r 9i s-s :a EE >o= 7=.9r5d 5e 6-S9EE EE €3;:ts4 Hx6isE I s;Ef Ei.qq€ r s ISSsi iEEEE; HoL !t c o i tr Eu: acoor, >Fi!xI j !s'$-E iEgEF* E Scan3?4 Nnrromhor Od ?ootr maw rJ) oo) (1, o. xoC!66 E6 &o- lo}ocxf 536- =obE>,i ([U, EEo_ol! l.- (!0 ^oro;? E9tfii 3_*fflfl9" .e€ E:2'=EtrEu- = o Yl t'l r)ooN F. o too- {.)t o .9o .9 E UJ E Scan335. November 04. 2005,max oo APPE,I{DIX 7 EQUIPMENT DESCRIPTION and MANUFACTURERS BROCHURES HYRUP PRODUCTION FACILITY NOBLE ENERGY INC. GARFIELD COUNTY, COLORADO Scan336. November 04. 2005 max Gas G3516Petroleum1085-1340 bhp V-16,4-Stroke-Cycle Bore - in (mm) 6.7 {170) Stroke - in (mm). ..... 7.5 (190) Displacement - cu in (L).. ... 4,210 (69)Aspiration ... Turbocharged-Aftercooled Capacity for Liquids - U.S. gat (L) Cooling System'. ... .. 54 (20s) Lube Oil System (refill) . .... 112(4231 Package Shipping Weight(Dry)- lb (kg) , , 17,670 (801s) 'Engine only. FULL RANGE OF ATTACHMENTS. Wide range of bolron system expansion attachments, factory designed and tested UNMATCHED PRODUCT SUPPORT OFFERED THBOUGH WORLDWIDE CATERPILLAR DEALER NETWORK. More than 1,500 dealer outlets. Caterpillar factory-trained dealer technicians service every aspect of your petroleum engine 99.7% of parts orders filled within 24 hours - worldwide Caterpillar parts and labor warranty Preventive maintenance agreements available for "repair before failure" options Scheduled Oil Sampling (S.O.S'nn) program matches your oil sample against Caterpillar set standards to determine: - internal engine component condition - presence of unwanted fluids - presence of combustion by-products SINGLE.SOURCE SUPPLIER. Caterpillar: - casts engine blocks, heads, cylinder liners, and flywheet housings - machines critical components - assembles complete engine Ownership of these manufacturing processes enables Caterpillar to produce high quality, dependable product.. Factory-designed systems built at Caterpillar ISO certified facilities r G3516 Standard and low emission ratings available Broad operating speed range and ability to burn a wide speclrum of gaseous fuels Cat" Electronic lgnition System (ElS) Bobust diesel strength design provides prolonged life and lower owning and operating costs. TESTING Prototype testing on every model: - proves computer design - verifies system torsional stability - functionality tests every model Every Caterpillar engine is dynamometer tested under full load to ensure proper engine performance. r WEB SITE For additional information on all your petroleu m power requirements, visit wwwcat-oila n dgas.com. CE Optional Equipment FEATURES Scan337. November O4 ?o|t1 mav LEHWo749-01 CATERPIL[AR' FACTORY INSTALLED STANDARD & OPTIONAL EOUIPMENT G3516 GAs PETBoLEUM ENGTNE SYSTEM STANDABD OPTIONAL Air lnlet Air cleaner - intermediate-duty with service indicator Remote air inlet adapters Precleaner Charging System Battery chargers Charging alternators Control System Governor - 3161 mechanical, RH with positive lock {PA53'19 & PA4871 only) Air-{uel ratio control (1A2031 & 1A2030 only 2301A speed control governor CSA 700 speed control governor 3161 mechanical governor Vernier and positive locking control (PA5319 & PA4871 only) Cooling System Thermostats and housing Jacket water pump Aftercooler water pump Aftercooler core for sea-air atmosphere Aftercooler thermoslats and housing Aftercooler core Thermostatic valve Temperature switch Connections Expansion and overflow tank Water level switch gauge Exhaust System Watercooled exhaust manifolds Flexible fittings Elbows Flange Flange and exhaust expanders Rain cap Mufflers Flywheel/SAE No. 00 flywheel Flywheel Housing SAE No. 00 flywheel housing SAE standard rotation Fuel System Gas pressure regulator Natural gas carburetor Low pressure gas conversions (PA5319 & PA4871 only) Propane gas valve and jet kits (PA5319 & PA4B71 only) A:.ltuel ratio interconnect wiring harness (LA2o31 & 142030) Fuel filter lgnition System Caterpillar Electronic lgnition System (E.r.s.) CSA ignition (PA5319 & PA4871) CSA ignition with AFRC (1A2030, 142031) lnstrumentation lnstrument panel, RH, 12 hole service meter Alarm module Customer communications modules lnstrument panel gauges (PA5319 & PA4871) lnstrument panel gauges f/u/w CSA electronic ignition system (1A2031 & LA2030) Lube System Crankcase breathars (top mounted) Oil cooler Oil filter, RH Oil bypass filter Shallow oil pan Oil sampling valve Oil bypass filter removal and oil pan accessories Sump pump Air prelube pump Manual prelube pump Turbo oil accumulator Lubricating oil Mounting System Rails, engine mounting - 10 in. (254 mm)Ra ils Vibration isolators Power Take-Offs Front housing, two-sided Front accessory drives Auxiliary drive shafts and pulleys Front stub shaft Pulleys Proteciion Electronic shutoff system PA5319 & PA4871: gas valve, explosion relief valves, status control box interconnect wiring harness Starting System Air slarting motor Air pressure regulator Air silencer Electric air start controls Electric starting motors - dual 24'volt Starting aids Battery sets (24-volt dry), cables, and rack General Scan33B, November 04, 2005.max Paint, Caterpillar yellow Vibration damper and guard (dual 23-inch) Flywheel inertia weight Guard removal Engine barring group Premium 8:1 pistons Premium cylinder heads G3516 cAS PETRoLEUM ENGINE CAIERPILLAH" TECHNICAL DATA G3516 Gas Petroleum Engine - 12A0'1400 rpm DM0107-04 DM5154-0'l DM5168-01 DM5't55-01 Arrangement Number PA487l w/oAFRC LA2030withAFBC PAs3l9w/oAFRC PA203l withAFRC Engino Power @ 100% Load @ 75% Load bhp (bkw) bhp (bkw) 1 o8s (809) 814 (6071 1151 (859) 863 (644) 1265 (944) 1340 (1000) 949 (708) 1005 (750) Engine Speed 1200 1200 1400 1 400 SGAC Temperature "F (.C)129 (54)1 29 (s4)1 2s (54)129 (54) Compression Ratio 8.0:1 8.0:1 8.0:1 8.0:1 Emissionsr NO, CO Total Hydrocarbons g/bh p-h r g/bh p-h r g/bh P-hr 2.0 1.8 a1 1.5 1.8 3.3 2.0 1.9 ?o 1.5 '1.9 3.1 Fuel Consumption @ 100% Load @ 75% Load Btu/bhp-hr (MJ/bkW-hr) Btu/bhp-hr (MJ/bkW-hd 7,450 (10.66) 7,414 (10.49) 7,534 (10.93) 7,591 (10.7 4l 7,548 (10.68) 7,541 (10.671 7,711 (10.91) 7,803(11,04) Heat Balance Heat Reiection to Jacket Water @ 100% Load @ 75% Load Heat Rejection to Aftercooler @ 100% Load @ 75% Load Heat Hejection to Exhaust @ 100% Load @ 75% Load Btu/mn (bkW) Btu/mn (bkW) Btuimn (bkW) Btu/mn (bkW) Btuimn (bkW) Btu/mn (bkW) 40,605 (687) 41,17 4 1724' 32,928 (546) 33,838 (595) 6,'r42 (109) 7,564 (133) 3,98.1 (62) 5,118 (90) 31,307 19421 39,980 (703) 26,9s6 (700) 29,8s7 (52s) 46,7 47 18221 47 ,B2B (8411 39,752 (699) 39,980 (703) 8,2461145l. 10,350(182) 5.118 (90) 6,995 (123) 45,155 (794) 48,0s5 (845) 32,359 (569) 36,624 (644) Exhaust System Exhaust Gas Flow Bate @ 100% Load @ 75% Load Exhaust Stack Temperature @ 100% Load @ 75% Load cfm (mYmin) cfm (m'/min) "F ('C) 'F ("C) 5,975 (180.0) 6,413 (181.6) 4,368 (129,1) 4,828 (136.7) 842 {.462). B4o (449) 820 G62t 817 {436} 7,179 (203.3) 7 ,684 (217 .6) 5,177 (146.6) 5,880 (166.5) 869 (465) 855 (457) 862 (461) 840 (449) lntake System Air lnlet Flow Rate @ 100% Load @ 7s% Load cfm (m'/min) cfm (m'/min) 2,264 112,81 2,433 (68.9) 1,681 (s2.1) 1,865 (52.8) 2,666 (75.s) 2,88s (81.7) i,928(54.6) 2,232l.63.21 Gas Pressure *at 100% load and speed HighHish Hish High Scan31Q Nnrromhor OA )Ofi( mav CATERPI[LAR" 73.31 (1863 G3516 GAS PETRoLEUM ENGINE GAS PETROLEUM ENGINE Note: General configuration not to be used for installation. See general dimension drawings for detail. BATING DEFINITIONS AND CONDlTlONS 131,41 (3339.2) DIMENSIONS Length in (mm)13i.47 (3339.2) width in (mm)68.33 (1735.6) Height in (mm)73.37 (1863.7) Shipping Weight lb (kg)17,670 (8015) Engine performance is obtained in accordance wirh sAE J1995, 1503046/1, 855514/1, and DlN6271/1 standards. Transient response data is acquired from an engine/generator combination at normal operating temperature and in accordance with lS03046/1 standard ambient conditions. AIso in accordance with SAE J1995, 855514/1, and DlN6271/1 standard reference conditions, TMI Reference No.: OMO107-04. OM5154-01. DM5168'01, DM5155'01 Malerials and soecilications aro subiect lo change wilhout notice' Conditions: Power for gas engines is based on fuel having an LHV of 905 Btu/cu ft (33'74 kJ/L) at 29.91 in. Hg (101 kPa) and 59" F (15" C). Fuel rate is based on a cubic meter at 29'61 in. Hg (100 kPa) and 60.1" F (15.6" C). Air flow is based on a cubic foot at 29.61 in. Hg (100 kPa) and77" F (25' C). Exhaust flow is based on a cubic foot at 29,61 in' Hg (100 kPa) and stack temperature. The lnternational System of Units {Sl) is used in this publica(ion' O2001 CaterPillar All rights reseryed.Printed in u.s.A.LEHW0749-01 (4-01) Snan340 Nnrrpmhpr O4 )OO5 mav ProposalTo: Noble ,n"rgy O For. Compressor Station NAt Proposal No.: 1J994465 Client Ref: Verbal A. ITEM IV - SKID MOUNTED GLYCOL RECONCENTRATOR ASSEMBLY One NATCO Model 5GR-550-KR-21015 PART NUMBER 99560005, 550,000 BTU/Hr Glycol Reconcentrator Assembly with the following equipment mounted, piped and interconnected : 1. One 24" OD x 8'-3" long Reboiler with 24" OD x 5'-3" lntegral Surge, Non- Code. Overall vessel length 13'-6". Assembly complete with: One B-5/8" OD, 300,0008TU/Hr removable firetube One 8-5/B" OD flanged, removable stack One Flame Arrestor with burner and pilot assembly One set of gas firing accessories including: Fuel Gas Regulator, Pilot Gas Regulator, Diaphragm Operated Fuel Gas Control Valve, 0-30# Pressure Gauge, manual shutoff valves and all necessary piping and tubing Two Kimray Model T12 Thermostats with thermowells, One for Reconcentrator Temperature Control and One for High Temperature Shutdown One 3" dial type thermometer with thermowell One tubular type gauge glass assembly with safety gage cocks and gauge glass guard h. One internalGas Sparging tube i. Two 1-112" Fill Connections, one in Reconcentrator section and One in Surge section with vent hole One 10-314" OD x 7'-6" long, Non-Code, Flanged Reflux Column Complete with: a. l" Ceramic Packing Three 3" x 1-112" x 10'-0" long Glycol/Glycol Hair-Pin Heat Exchangers, 250,000 BTU/Hr Heat Transfer Rating One High Pressure glycol filter assembly complete with one filter installed and one replacement filter One KIMMY Model 21015PV glycol powered pump mounted and piped, complete with speed control valves and block valves All piping is schedule 80 and all tubing is steel or stainless steel with steel tubing fittings Complete assembly is mounted on a structural steel skld, 4'-6" wide x 18'-0" long d. b. C. d. e. f. g. 3. 4. 6. 7. NAT'CO Proposal Page 2 of 4 eNneddnffiIPl company Snanldl Nnrromhor {\4 )o.O6 mav 2 5. ProposalTo: Noble en"rgy O For: Compressor Station Client Ref: Verbal INSULATION: The reboiler section of the Reconcentrator and the removable Reflux (Still) Column are insulated with 1-112" Easy Wrap and covered with an aluminum jacket COATING: Complete exterior of Assembly is commercially blasted and painted one coat Mesa Tan Primer One (1) NATCO Part Number 99550248 23'- 6' OD x 25'-6" shell length x 1440 psig working pressure, ASME Code Constructed and National Board Stamped, Glycol Contactor Tower complete with lntegral Scrubber, Outside Gas/Glycol Heat Exchanger and complete as follows; 1. Vessel lnternals: Eight (B) Bubble Cap Trays on 24" spacing lnlet Gas Diverler Full Diameter 304 SS tower, 9# density ,oO Proposal No.: 1J994465 B. One (1) 3" 600# ANSI RF flanged One (1) 4" Hammer Union One (1) 1" 6000# threaded coupling One (1) 3" 600# ANSI RF flanged One (1) 1" 6000# threaded coupling One (1) 1/2" 6000# threaded cplg One (1) 1/2" 6000# threaded cplg One (1) 1" 6000# threaded coupling One (1) 1" 6000# threaded coupling One (1) 1" 6000# threaded coupling mesh mist extractors in scrubber and . GAS INLET - LLC . RELTEF , GAS OUTLET - LIQUID OUT . PRESS GAUGE - THERMOMETER - GLYCOL IN - GLYCOL OUT - GLYCOL DRAIN wire d. 2. Vessel Vessel a. b. c. d. e. f. .).)- Extra heavy chimney tray and gas riser for longer life Externals: Welded steelskirt and base plate One External Gas/Glycol Heat Exchanger Connections: g h i. j 4 Accessories Furnished : One (1) INVALCO model CTU4155 liquid level control with integral sight glasses One (1) INVALCO model DSG-160 diaphragm operated liquid discharge valve, with 1/4" SS trim One (1) ASME 1" x 1" threaded safety relief valve set at 1440 psig One 3" dial type thermometer with thermowell a. b. NATC)O,Proposal Page 3 of 4 eMf,cosnilFlcompany Scan342. November 04. 2005.max Proposal To: Noble fnurgf For: Compressor Station O Proposal No.: 1J994465 Client Ref: Verbal e. f. One (1) 2-112" dial, 2000# pressure gage with 114" 6000# isolating valve One (1) lot instrumentgas tubing and tubing fittings to hookup Level Control and Dump Valve One Flex Hose for hookup of contactor to Gas/Glycol Heat Exchanger One set of gaskets, studs and nuts for connection of Gas/Glycol Heat Exchanger to Contactor Gas Outlet Contactor to Reconcentrator Hookup Kit o. h. i. 5. Coating: Complete exterior of vessel is commercially blasted and painted one coat Mesa Tan Primer ITEM IV - SKID MOUNTED GLYCOL RECONCENTMTOR ASSEMBLY NET PRICE, EX-WORKS NATCO MANUFACTURING FACILITY $43,743.00 US Deliverv: ln stock subject to prior sale. o NATCO aM.FcacnouFl company Proposal Page 4 of 4 Scan343. November 04. 2005.max e5 h:dorr f dctry =f co (ut-1' o c)g o. E ((, X Lr.J (g o E Gt-t) .go 3otr a U' 0)ool- rL 6E9Cx!()A iH €E Lo!sE(HO IA Scan344. November 04. 2005.max cB EE4 O\E EdE l- Ir -4.- I I lcq96 -LL'E^ Av I t_ Ut" eJ-E qY(Jri ooN CO ca .-.; otn Id o o c.)V' uoo C3 o il.o (.) t-ot) I "uco(J lt I .3 F€ =d 0) Etr) \o '5Lco 4)! il ,!,c I atr ? O L .= )l ll-o-(i I c--I \=z tt O lstol> IEto l. loi:lal.ilsl-lG t\, It IO ls iotzio lo l3 I I E a $ o o2.9Y P) trr -E o .= ceEE E;ggg 'tr 6)aii - o. 5-o(U=!u€ gp= ,P S2 ^'3*. E E6p =ayog oE6o,5 io> h 5df EEt g s - >o ,:Y 6P> FE{- u ofcLjYoeoo)o o_ - a -. o, o x,;;.Ee33;.s;e f, e BEEE{ I Et66)).Y;7c f1?f 3Hgi,re p #iFtt[sitg s 3t fi5, ZEzFEmms o 0)ON N-C.b-+ tf ,\oiD =(Do.= 4ic,)(o ooo(l,g) o) oo oe-szXtA=f,!l o-oLK PPo i|E -OOoddo..:.b<()o o-i :+boolf) a +<\o = cw *r G H t4 \ o=.Eq,T- o# Qa od I(! o-o- o o a o c co (L)F -m o o o -c B a o t,o TL coo- tro O 0) Eo :E a o- Ef 0- Jo+ol* Joo& tlo3 j o- tO o N U;(L Ef o- Joo o IL o ? I = a ; = th o,co'J € c) tr.9 = !_t 0 (J { oo E 2 d^a9(LFpY -d ;E ul O a.o F a.J oO.roo oor; oN F Ue T]J J B o N o N . 11.1 3g :c (, N:c o .uI 63 No (, N c; (, IUFaa<a0l uJUELO-o ooo oof) ZaOa6 Lil-ul(rOO- oo O =o- aoaulo o-o o N IU(9 ErO U) o F =o_a 6 o N u, 6- F- c o- UNa o N N N .-_, "2@roxi>,i or c EgEPo = : !o>4PE.+ .,.i:.9O - { N o 9u-l-cj€:E ',aE;",3 I p ff E Ei;Pd L (, iZ Yao-N KIMRAY, lnc.GLYGOL ENERGY EXGHAI{GE PUMPS Oklo. City, OK 'rq5 INTBODUCTION: The Glycol Energy Exchange Pump, "Pressure Volume" or 'PV-Series" Pump was developed in '1957. The initial consideration was a pump that would utilize the energy of the wet glycol at absorber pressure as a source of power. Within the confines of a system, energy can neither be created nor destroyed. Energy can, however, be stored, transferred, or changed from one form to another. The PV Series Pump transfers the energy available from the wet glycol, at absorber pres- sure, to an 'equivalent' volume ol dry glycol at reboiler pressure. ln order to circulate the glycol, additional energy is needed to overcome friction losses within the pump and connecting piping. This additional energy is supplied by gas at absorber pressure. The pump was designed as double acting with a maximum working pressure of 1500 psig with a factor of safety of ten. Corrosion and wear dictated use of the best materials available. These materials include stainless steel, hard chrome plat- ing, nylon, Teflon, stellite, and'O'-rings specially cornpounded for glycol service. The pump contains two basic moving parts, a Piston-Rod Assembly, and a Pilot Piston. Each actuates a three-way D- slide. t Cmfiguralio d GlFd Arrp R a trda.rt d Kimray. lrc. G:1o.1 lssued 12'83 Scan346, November 04, 2005.max - *_',a*tslr\,*rP KIMRAY, lnc.GLYCOL ENERGY EXCHANGE PUMPS OKLA. CITY, OK PRINCIPLE OF OPERATION: Actions ot each ol the lwo basic parts ot the pump are com. pletely dependent upon the other. The pilot D-slide actuated by the Pilot Pislon alternately teeds and exhausts absorber pres. sure lo the power cylinders at opposito ends ol the piston-Rod Assembly. Likewise, the Pump D-slide actuated by the pislon- Bod Assembly alternately feeds and exhausts absorber pres- sure to opposito ends ot the Pilot Piston. The force to circulate glycol within the dehydration syslem is supplied by absorber pressure acting on the hrea ol th-e piston Rod al its O-ring seals. The area of-lhe piston Rod is approxi- mately 20 percent of that of the Piston. Neqlectino pumo liiction and line losses, lhe resultanl lorce is sutficient to fioouco a the. orelical discharge pressure 25 percent greater ihan absorber pre-ssure. The lheorelical discharge preisure, lor example, al 300 psig absorber pressure would-be 1875 lbs. This lheciretical"over-pressure" would develop aqainst a bbcked discharoe line but is not sutficient lo cause Oamiqe or creale ahazard. ' Approximately 25 lo 30 psig pressure is required lo overcome pump lriction leaving the addilional "over pressure" jor line loss- es and circulation. ll is recommended that these losses be held to approximately l0 percent of the absorber pressure or as noled in catalog. Two Speed Control Valves are provided to regulale the llowo, wet glycol and gas lo and,rom the power cylinders. Reversing lhe direction of l,ow through the Speed Conlrol Valves provides a llushing action which cleans the valve orifices. It the wet glycol, reiurning lo the pump lrom the absorber were lo be complelely lill the cylinde( no additional gas would bo needed. However, the wet glycol will only occupy approxi- mately 65 percent of the total volume of the cylinder and con- necling lubing leaving 35 percenl to be ,illed by gas lrom the absorber. This gas volume amounls to I.75.C.F. per gallon ol dry glycol at 300 psig absorber pressure and B.35.C.F. al 1500 psig and may be considered as continuing power cosl for pump operalion. This gas can be utilized in the regeneration process ol the dehydrator for "rolling" and or "stripping" purposes. lt may also be recovered in a low pressure glycol gas separator and used lo lire the reboiler pressure glycol gas separalor and used lo lire the reboiler. By supplying some absorber gas to the cylinders, the wet gty- col level is maintainad at the wet glycol outlet connection on tho absorber and eliminates lhe need ol a liquid level controller and its atlendent problems. Excess liquids such as hydrocarbons are removed from lhe absorber at approximately 55 percent o, ths pump rale, reducing the hazard o, dumping a largo volume of hydrocarbons into the reboiler as would be the case with a liquid level controller. DffY Gt\rcOL DISCHARGE WET GAS INLET HI.PRESSURE FILTEF WE T GLYC TO REEOILER INSTALLATION: A number o, considerations should be made wilh regard to pump installation since il is the "heart' ol a dehydra- lion system, Il is a moving mechanical devico subject lo wear and w,ll ultimately need repair. Location of the pump is very important. Easl access to the pump for repair or exchange can save lime and trouble. Test conneclions (1/4' NPT with valve) located on the piping to and trom lhe pump permil a last means ol trouble shooting pipe restrictions or blockage. Filters, which are discussed lalel should always bo installed in the wet glycol piping between the absorber and pump and in the suction line lo the pump, wilh provisions made for maintenance of the lilters. Suclion piping should preierably bo large enough to permit a positive leed to the pump. Feed pressure must be more than 4 or 5 inches of Hg yacuum to prevenl pump cavila- tion PLUG VALVE L h lalclos. yhb punrh n rylohon. KIMRAY DFY GLYCOL srjcTroN ( Mor.zOO'F ) GLYCOL I LOW PNESSURE irtiin- - ! Wher8 two or mote pumps are manitolded logether, the tolal capacity must be considered in the piping design. Also, a mani- told should be designed to provide oach pump with its "Fairshare" ol the wet glycol (rorn lhe absorber. lt is not neces- sary that the proportion be exact. Pumps with lower "pumping ratios" are avallable to provide addillonal energy lor pressures below 300 psig; bul is it better not to use those pumps at pressures above 400 or 500 psig because ol excsss gas consumption. Conversion kils are available to change standard pumps to "SC" pumps with declin- ing lield pressures. PUMP SHUTDOWNS: Pump shut.down mechanisms, which require no adiuslment and are conlrolled by the discharge ol dry glycol, are available. The Kimray ASD Shutdown is a check device which permits pump operation as long as dry glycol is being dis- charged from the pump. (See page 10.26 for description o, operation.) I Conliguralion o, Glycol Pump is a rademilk ol Kitray. lnc G:10.3 lssued 1 2/83 PLT,,G VALVE 'c' MAX. TEllP. 200. F. MAX.W.P. l5OOp.:.i. Al filhngs, n/tut,volws, md slroiec lwn hqc ore lo k funshed b, cuslomcr- ELEED VALVE "B' F!MP Scan347 Noveml-rer 04 ?OO5 max ABSORBER KIMRAI lnc.GLYC0L ENERGY EXCHANGE PUMPS 1500 Lb. W.P. oklo. ciry, oK HEAT EXCHANGERS: Sullicient heat exchange is necessary to reduce dry glycol suction ternperature to at least 200"F, prelerably to .150'F. SPLIT DISCHARGE CHECK VALVE BLOCK: Kimray Glycol Pumps are available with check valve blocks for split discharge lo serve lwo absorbers on a dehydralion unit. See pago 10.29 for a description. VITON "O" RINGS: Viton'O" rings lor all moving seals in th Kimray Glycol Pumps are available. Vilon repair kits can be ordered for pumps already in operalion or new pumps can be ordered with viton "O" rings at additional cosl. Viton "O' rings are recommended lor use when liquid hydro- carbons are round in the gas, lor CO2 service or lor elevated operating temperalures. Under normal conditions (without ths above problems) viton'O'rings will nol give as long ol a service lifo in the pump as standard Euna-N "O" rings. SYSTEM PBESSURE DROPS: The Kimray Glycol Pumps are designed lo operate by using the energy lrom the wet glycol and some additional energy in lhe form of gas at absorber pressure. Excessive pressure drops in the lines connecting the pump to the system can cause lhe pump lo run enatically or slall. The lollowing conditions should be designed into the system lo assure proper pump perror- mance: DRY GLYCOL SUCTION LINE: Size lhe suction line, low pressure filter and heat exchanger such thal the pump will have a posilive pressure at the suclion inlet when running at lhe maximum rated speed. This line may need to be larger than lhe pipe fitting on the suclion check valve block. (Seo pipe conneclion sizes on page 10.28.) WET GLYCOL POWEB LINE: Recommended line size is lhe same as the size ol the pipe connection lor the given pump. (Page 10.28) The pressure drop across the high prossuro lilter is a lactor in considering lhe total system pressule dIop. DFY GLYCOL DISCHARGE LINE: Rocommended line size is the same as the size ol the pipe conneclionlor the given pump and the absorber should be lull opening lo lhe recommended line size. WET GLYCOL DISCHARGE LINE: Becommended line size is lhe same as the size of the pipe conneclion lor th egiven pump. (Page 10.28.) lf a glycol gas separator is used, the pressure maintained on leh separator must be considered in the total system pressure drop. Also, heat exchanger coils in accumulalor tanks also add lothis pressure drop. ISOLATING VALVES: All plug, gate, or blocking valves should be lull opening lo lhe recomended line size ot lhe given pump. ll a posilive feed is supplied to lhe pump at the dry suction inlel, lhe lolal system pressure drop will be the sum ot the lol- lowing pressure drops: 1. The pressure drop belween lhe absorber and the pump in the wet glycol line. G:10.4 lssued 1 2/83 2. ThB pressure drop between the pump and lhe absorbet in the dry glycol discharge line including any pressure required to open and establish lull llow in any check valves. 3. The pressure drop belween the pump and the reboiler (at atmospheric pressure) in lhe wet glycol discharge line. This includes the liquid head to the reboiler, heat exchanger coil, and/or the pressure maintained on a glycol seperator.k The sum o, these pressure drops gives lhe lotal "system pres- sure drop". The graphs on pages 10.11-10.15 give lhe maxi- mum tolal system pressures and lheir et ecl on pump output. Exceeding the total allowable syslem pressure drop will cause the pump lo run erratically or to stall. To determine it a problem exists in an operating dehydralion syslem, slowly open the speed conlrol valves on lhe pump until il runs at the maximum recommended pump speed. (See graph page 10.8.) ll the Pump cavitates belore reaching the maximum pump speed, the suction line is restricted. ll lhe pump will not run at the maximum rated speed, lhen lhere are probably reslrictions in one or more ol lhe other three connecting lines. FILTERS: Fillers should be used on every dehydrator foI protection ol bolh lhe pump and reboiler. Many pumps are soverely damaged in the ,irst minutes or days of operalion ,rom llow line and ves- sel debris. Reboilers have been known lo be lilled with sand which had to firsl pass through the pump. Filters should give proleclion ,rom 25 to 150 micron particle sizes depending on the specilic condition. The disc type, microin lype, and sock type have all proven very satisractory if they are properly maintained. Some metal lilters are equipped with a cleaning device which should be operaled daily or at leasl every few days as experience may diclale. Sock fillers must be replaced at regular intervals. Preventativo mainlenance on these lillers will save many dollars in major pump and rsboil er repairs plus lhe reduction o, costly down time. A spring loaded by-pass on the liller is not recommended. lt is better lor the pump to stall duo lo lack of power lhan be exposed lo dirt and grit lrom an open by-pass. Always install a high pressure liller between the absorber and the pump. A liltor on the wet glycol discharge of lhe pump will protect ths reboiler but does nolhing lor lhe pump. A low pressure liltet on lhe pump suction prolects against metallic particles from a new reboile, and ils connecling piping. Filtets will also keep the gly- col lree ol heavy tars and residue from evaporaled hydrocar- bons and rosinous compounds caused by polymerization of the glycol. Sock type tilters are probably best for this type ol filtra- tion bul should be changed rather llequonlly. ln addilion lo using lilters it is otlen necessary to make a chemical analysis of lhe glycol, not only for pump prolection bul lor better dehydralion. Organic acids in glycol are produced kom oxidation, thermal decomposition, and acid gases lrom lhe gas stream. These acids cause sorrosion in lhe system, and dissolve the plating on pump parls in a short lime. Glycol acidity should be maintained between a pH ol7 lo 9. Alkaline amines are usually recommended to control lhe pH value because they will neulralize any acid gasos presenl and are easily regenerat- ed. Scan34B, November 04. 2005.max KIMRAY, lnc.GLYCOL ENERGY EXCHANGE PUMPS 1500 Lb. W.P. oklo City, oK Anolher glycol contaminate which causes pump problems is salt. Salt water which conlinues to enler a dehydration system soon producas a super saturated condition in the reboiler. This results in salt deposits in the lines and in th€ pump as the hot glycol is cooled. A complote cleaning and washing of lhe entire system is required to remove the sall, OPERATION: A new pump or new dehydrator should be put into operation by lirsl bringing the glycol circulation and operating tgmperature to an equilibrium condition by using 300 to 400 psig absorber pressure. This can be done with or wilhout gas ,low. ll it is easi- er lo slart up under a nojlow condilion, only enough gas need be supplied the absorber lo maintain lhe pressure. In most instances the purnp will pick up its prlme wilhout help and should do so in a few slrokes. lf the pump does nol prime imme- diat6ly, the dry glycol discharge should be opened to atmo- sphere until glycol discharges trom both cylinders. When equi- librium has been established, the pump should be stopp8d an lhe absorber pressure increased lor operation. pump speed can then be reeslablished lo lhe desired rate. The maximum operating temperature ol the pump is limited by the moving "O'-ring seals and nylon D-slides. A maximum ol 200 degrees as recommended. Packing life will be exlended considerably at 1 50 dogrees. Always stop the pump when tha pump when the main gas flow is lurned oft. A pump which conlinues to circulate with no gas llow elevales the complete dehydralor temperalure, and in time to reboiler temperature. ll a pump has been deactivaled lor several months, the check valves should be removed and inspected before aflempling lo operate the pump. Tho pump startup should be similar to that ol a new pump by firsl bringing the system to equilibrium. TROUBLE SHOOTING: lf a glycol pump has been operaling in a clean system il is very likely lhat no major service will be required for ssveral years. Only a yearly replacement o, packing will be required. Normally the pump will nol stop pumping unless somo inlernal parl has been bent, worn, or broken, or some foreign object has ,ouled the pump, or lhe system has losl ils glycol. A pump which has been running wilhout g,ycol lor some time should be checked belore returning to normal s€rvice. Probably the pump will need al least new "O"-rings. The cylinders and piston rods may also have been scored ,rom the 'dry run' Following are soms typical symptoms and causes. These are presenled to assist in an accurate diagnosis of trouble. SYMPTOMS 1. The pump will nol operale. 2. The pump will start and run until lhe glycol relurns lrom the absorber. The pump lhen slops or slows appreciably and will nol run at its rated speed. 3. The pump operates until lhe system lemperalure is nor- mal lhen the pump speeds up and cavitales. 4- The pump lopes or pumps on one side only. 5. Pump slops and leaks excessive gas from wet glycol dis- charge. 6. Erratic pump speed. Pump changes speed every lew min- utes. 7. Broken Pilol Piston. CAUSES 1. One or more ol the flow lines to the pump are completely blocked or the system pressuro is loo low for standard pumps (below 300 lbs.) uso "SC'pumps below 300 lbs. 2. The wel glycol discharge line to thereboiler is restricted. A pressure gaug€ installed on teh line will show the restriction immedialely. 3. The suction line istoo small and increase in temperature and pumping rale cavitates the pump. 4. A leaky check valve, a loreign obiect lodged under a check valve or a leaky piston seal. 5. Look for metal chips or shavings under the pump D- sildes. 6. Traps in the wet glycol power piping sends alternate slugs of glycol and gas to the pump. 7. lnsutlicient glycol to the Main Piston D-slide ports. Elevate the control valve end of hle pump lo correcl. G 10.5 lssued 1 2/83 Scan349, November 04. 2005.max KIMRAY, lnc. "PV" & "SC" SEBIES GLYC0L PUMPS 1500 LB. W.P. Oklo. City, OK "PV" SEBIES GLYCOL PUMPI Catalog I Model Number I Number I CapacityI Gal / Hr. Irri^ Irr".. I WorkingI Pressure I r,,ri^ I r,,1"' GAA GAD GAB GAF GAH GAJ 315 PV 17r5 PV 401s PV 9015 PV 21015 PV 45015 PV 3 8 12 66 166 '13 40 40 90 210 450 100 300 300 300 400 400 500 500 500 500 500 500 "Maximum outpul is affected by system pressure drops. See system operation parameter lor maximum output curves. APPLICATIONS: Circulaling pump lor gas glycol dehydrators Circulating pump for gas amine desulphurizers FEATURES: Eliminates absorber liquid level controls No auxiliary power supply required Low gas consumption Completely sealed system prevents loss glycol No springs or toggles, only two moving assemblies Hydraulic "cushioned" check valves with removable seats ol hardened stainless steel PUMPS AVAILABLE: tConliguration ol Glycol Pump is a trademark o, Kimray, lnc .SC' SERIES GLYCOL PUMPS Catalog Number Model Number Capacily Gal. i Hr. Working Pressure Ma Min.Max. GAC GAG GAI GAK 2015 SC' 5015 SC' 10015 sc' 20015 sc' 8 12 22 60 ?o 50 100 200 100 100 100 100 500 500 500 500 NOTE: To order a Pump with Viton O Rings add I to Catalog number. Example: To order GAA with Viton O Bings, specily: GAA1. OPEBATION: Malerials lor the vital working parts have been selecled for greatest weat resistance. These malerials include slainless steel, hard chrome plating, satellite, nylon and tetlon. Moving "O' Ring seals are compounded specilically ,or €thylone glycol service. A complets operational check is given each pump alter assembly. "O" Hing sealed check valve darls are standard in all except the model 315 PV, Teflon sealed darts are avaitable. Capsule type ball checks are used in the 315 PV and are availabls for 1715 PV. 2015 SC and 4015 PV. 'These pumps are designed lor operating pressures between 100 and 500 psig maximum design pressure for all models is 1500 psig. MAXIMUM DESIGN PRESSURE FOB P.V. AND S-C. MODELS IS 15OO PSig G 10.6 lssued l0/94 Scan350. November 04. 2005.max l KIMRAY, lnc. G:1O2 lB$u6d r2l83 6LYC0I PUmPS 1500 Lb. 1il.P.Ok[o. City, OK --!oacd {ao/roi Ldixt 1_/ \- i?lt 6$ro/ {hrtorrc W &tryPisnnAs€ondy W Wet 6bcd lron Aborbt( HiS Prdsgtra) l:1.1 Wtt 6Otd to frrhoilc/{Low Pressara) Nffi Ory Glycd fmn Rcbotla ( Lw fteevrc) p$@ Ary Oyor tu 4bsorbat ( High Praseurt) fiixttrlt thai iinr 6*uln# I OPERATION: Th€ Kknray olycol pump is doubls adtrq, po$sr6d Dy l bt Glycd arul & sna[ qran$y ot ga$ at absorbor rrossuro {B€d). 1'lollolr donol€$ wet Glyed (Bluq) ls bolng pumped lo iho sso{Oor. Gioon lB Dry Glllool orrffon trofi ho robolk{. Wel Glycol (Flod) trom the aD8orber no$/s through port t4 ard ls thrcUlod througfi the SPEED GOHTROT VALVE to lho btt end oI the Pump Plston A8sombly, movlng thb acsernbly fifin btl to r{ghL Dry Gtycol {Biu6) b bolng pumpod Irom t}|e lelt cyhder to thB aDso{bar whll€ th€ rbfrt cyilnds is b€i{o flfiod wih Dry Gvcol (Gr6en) lrom ths rebote. Al ho sarno thns Wbl Gly(Dl (Yoilo!^,) is dlscheroiilo lrom tho rlght 6nd ol &o Pump Pl6'trDn Assombly to a lo\a prossure or alllrcEpheilc 6ydem. A6 ltla Purnp Pl8to{r Ar$ombly noa,6 tho ond o, lts $lroko. lhe POSITKJN FING on the PISTON RoD corlacls tho rlght ond ol tho ACTUATOF. Fu.the( mot/omonl io th€ rlght mo/o3 tho ACTUAToR snd PUMP 'tr SUDE Io uncovor pod tl and oommunlceto ports il2 and il3. Thl$ exh&rslB W€t Glyco} (HBd) to ths rlglt ond o{ the PILOT PIS- TON. Thl6 causs tiB PILOT PISTON snd Pll-OT 'D'SLIDE to b€ drfvsfi lrom rlgfit to lelt ln lt$ new po*lkm trl6 PILoT 'o' SLloE uncovors pon #5 and cofnmunhab$ porb #4 and r€. THb exhausts vrbt Glycol (Bod) lrom ltle lolt ond of the Pump Pblm Assembly Urrl)ogh ports ld ard tg to lh8 low pr€6s(l.e lr'Yel Grycd (\blo{n) syslsm. Porl fS ('*rhn was ccmmuni@led wlth pofi ,B) now aomiis !ir6l Gucol (Bod) through ffte rlgM hBnd SPEED CON' IROL VALVE to ths t$li erts ol tho Purnp Plslafi Assernbly. Thc Punp Pl6ton Aesombtyiy nollr sldls rlo €iroxo lrom rt0hl to bn, R lovr aDovo ptocsdurD rorrordng <Jireclirre c{ lbw.. t Coroudhn d 6l}&d Purp 6 r trqdm* d Kmny kr W 0:!ar< ^:{Cxh,yt \f1 "" Friday, November 04, 2005 (B).max KIMRAY, lnc. "PV" & "SC" SERIES GLYC0L PUMPS 1500 LB. W.P. Oklo. City, OK INSTALLATION DIAGRAM Max. Temp.200'F. Max. W.P. 1500 psig ORY GL}TOL OISCH^RGE FLUG VALVE "0" BLEEO VALVE PLUG VALVE L hrclclMytlcpumpithWohoD. WET GLYCOL TO REBOILE R ORY GLYCOL SUCTION ( Mor.2OO'F ) All liltings, fillers. valves and slrainers shown here are to be furnished by customer l'll ABSORBER'; 1: HI.PRESSUFE FILTER INSTALLATION: For maximum purnp life a high pressure liller should be installed in lhe wet glycol line between lhe absorber and pump. Also a low pressure lilter or strainer is recommonded lor the dry glycol suction line between the accumulalor and pump. Adequate heat exchangers must be provided lo keep lhe lemperature of fluid llowing through lh6 pump bslow 200'F. The lollowing lilter and strainer line sizes are recommended minimum: 315 PV . . .. .1/4" NPT1715PV ....1/2"NPT 4015 PV & 2015 SC . . .1i2'NPT 9015 PV & 5015 SC . . .3/4" NPT2101sPV&10015SC.... .......i',NPT 4s015PV&200t5sc . .11/2" NPT Bleed valves "A" and "8" are required ,or removing pressure lrom the pump to allow inspection and repair. Bleed valve "A'is also used tor priming as described below. The plug valves and unions permit the pump and lillers lo be easily isolated or removed lor inspection or repair. LOW PRESSURE FILTER OPERATING PROCEDURE: 1. Closo both speed conlrol valves, bleed valves "A','8" and plug valve "C". 2. Open plug valves "D" and "E"- 3. Pressure absorber lo about 300 psig. 4. With plug valve "C" closed, open bleed valve "A". 5. Slowly open both speed control valves unlil pump is running about 1/3 raled max. strokes per minule. Count one stroke lor each DISCHARGE ol PUMP. When dry glycol discha.ges lrom valve 'A" on each stroks, ths pump is primed. Close valve "A'and open valve "C". Readiust speed control valves to 1/3 rated max. strokes per minulo and continue operating pump until wet glycol returns {rom lhe absorber to lhe pump. This will be evidenced when the pump tries lo meter liquid lhrough the speed control valves instead of gas and causes lhe pump to slow down. Close both speed control valves. 6. Bring absorber 10 lull operating pressure. 7. Ad.lust speed control valves for desired rate (see capacily charl). 8. lnspect and clean lillers and strainers periodically. 9. For prevenlive mainlenance, "O" Hings should be roplaced annually. To check 'O" Bing seal, close valve 'C". ll pump conlinues lo run, seals should be replaced. SYSTEM SHUTDOWN: 1. Close plug valve "D'Allow pump to stop running 2. Close plug valve "C'and "E' 3. Bleed pressure lrom bleed valva'A'and'C" lConliguralion ol Glycol Pump is a trademark ol Kimray. lnc G. 10.7 lssued 10€4 Scan351, November 04, 2005.max WEI cas INLET KIMRAY GLYCOL R'MP KIMRAY, lnc ,.PV" & "SC" SERIES GLYCOL PUMPS 15()(} Lb. W.P.Oklo. City, OK CIRCULATION RATE GRAPH o so too tso 200 250 300 350 400 450 MAXIMUM GALLONS PER HOUR OUTPUT 'lt ls not recommended to atlompt to run pumps at spe€ds less or orealer than those indicated in the above graph. GAS CONSUMPTION Operating Pressure --p.s.i.g 300 400 500 600 700 800 900 1000 100 1200 1300 1400 1500 40 IJF) =c. 3o T!o al!:ao^^tavF an o trJ trJo-.-(4lu o- DI 0 Cut. Fl./Gallon @ 14.4 & 60"F.2.7 2.3 2.8 3.4 3.9 4.5 5.0 b./6.1 7.2 7.9 8.3 Cenler Lne, olr ccffeclrffi Model Number 'PV" Series "SC" Series Dimensions, lnches GHJ 1715 PV 5'^ 5"i" 5'/, 3'l', l'h 3'/, 7'1, 10'/, 10/'r 9Yr 15 1'l, 4015 PV & 201 5 SC 5'/, 5"/'t 5t/, 3'ls 1'h 3'h 7'1, 10ti 10'/'c 9t/r 15 2'1, 1'1, 90r5 PV & 501 5 SC 6'/, 8'/,t'/, 6'/,ltl' 4'1, 8Y, 13'/n 13%r 11'/, 20 2'h 210r5 PV& 10015 SC 73h 1}'l,t'lt 7 5'h 2'1, 5% 9'/r 14y. 16Y, 13 24 3'/,, 2'h 45015PV&20015SC 10r/, .l4t'/, 9 6'/, 2'h 6'h 11r[ 19 2l'1, 16'h 34 3% 3'h Model Number Max. Cap.Size ot Pipe Conneclions Mounting Bolts Approx. WeightG.P.M.G.PH, 1715 PV .b/40 '/a'N.P.T.3/g" Dia.66 Lbs. 4015 PV .67 40 r/r'N.P.T.3/s" Dia 66 Lbs 9015 PV 1.5 90 3/{" N.PT.1lz" Dia.119 Lbs. 21015 PV J.f,210 1'N PT tlz" Dia 215 Lbs 45015 PV 1C 450 1!/2" N.PT 'lz" Dia.500 Lbs. G10 8 lssued 1 2/83 lconliguration ol Glycol Pump is a lrademark ot Kimray. lnc. Scan352, November 04, 2005.max O lcr rynoml ol PrJon RoC -..| r__ i _.-_ * 'L=:cl u;s1 Gtyco l^let i - ,' ABC MN KIMRAY, lnc.GLYGOL PUMPS 1500 Lb. W.P. "SC" Series Oklo. City, OK SMALL BORE CYLINDER PUMPS FOR LOW PRESSUBES o 50 loo r5o 200 250 MA}CMUI{ GALLONS PER HOUR OUTPUT ' lt is not recommended to attempl to run pumps at speeds less or greater than those indicated in teh above graph. GAS CONSUMPTION Operating Pressure-p.s.i.g.100 200 300 400 Cu Ft./Gal. @ 14.4 & 60'F.10 1.9 ta The.SC'(small cylinde4 Series glycol pump was designed lo extend the lower operating pressure o, the "PV" Series pump downward lrom 300 p.s.i.g. loo100 p.s.i.g. Due to increased gas consumption il is recommended to use lhe "PV" Series pumps at pressuras greater than 400 p.s.i.g. Any Kimray "PV" Series glycol pump, excepl the model 315 PV can be lield converled to a 'SC" Series pump of comparable size (see comparative lable belo|). Likewise, "SC" Series pumps can be converted lo "PV" Series pumps. The parts required lor lhese conversions are stocked in kit lorm. To order conversion kils specify; (existing pump model) conversion kit to (converted pump model). Example:"4015 PV Conversion Kit lo 2015 SC.', COMPABATIVE TABLE "PC" Series Model No. "SC" Series Model No. 1715-4015 201 5 SC 90 t5 s015 sc 21015 10015 sc 4501 5 2001 s sc G10.9 lssued 1 2/83 50 )?;..4C Gf 8:oF Io %zo a) t0 Physical demensions ol ''SC" Series pumps re the same as the comparable'PV' Series pumps. See page 8. PARTS REQUIHED TO CONVERT FROM'PV" TO SC'SERIES PART NUMBER PAFIT NAME Quantity Required 4015 PV to 2015 SC 9015 PV lo 10015 SC 21015 PV to 10015 SC 45015 PV to 20015 SC Cylinder Liner 2 2108 2373 2412 +1 505 Piston 2 1 506 776 1 075 1 508 Piston Seal Retainer z 1 509 1510 1511 1512 Piston "O" Bing 2 156 773 774 329 Back-up Rlng 4 1513 1457 1 458 +772 "o" Rinq Z 154 154 155 1107 Lock Nut (Piston)2 906 175 1 140 Cylinder "O" Ring 2 773 774 200 'The piston is the nut lor this model and is turnished with a socket head set screw. dFull cylinder only. fModel 20015 SC only. requires 8, No. 772 Back-up rings. Scan353, November 04, 2005.max KIMRAY, lnc.GLYCOL PUMPS Oklo. City, OK DESIGN PRESSURE: 1500 lbs. tEt MODEL 21015 PV PUMP s +Conliguration o( Glycol Pump is a trademark of Kimray. lnc. WORKING PRESSURE 300 lbs. Minimum 1500 lbs. Maximum G 10.21 lssued 1 2/83 =E E I 9 F ! a, s$ IF 5 s t I I ! u\ R ) t t t' :r'i:'I tIIIils';t i; .I !"Y(t I Ei iiii 5i }iii i iRT !'$I I 6S?iHi da 3 I ,si!* I{Tac is I t ) s o It T I $I Pt if 3r ei3 Ssti sisffr,o HB [$ Ie t I! si 6 -si $ i3a' !S5 l" 5r s !l! i!i!E t :I ti Iq to! \' ti c 6 t IItt R T::tt tntt'f .!I F:. ' . I te ii s{$ i;nis s i i;; g $ p !i i.r,ii i BB r! i t{Iii i$ I* a $:.r I B & Io ic ttc i R t u\ 5si tL- ,aeEi. isi = {' xii+ !!l- $lq 9 t,t{ i isli iG si i tr I @ !!.; lF UU t t !1 :! loC-E ES-P I tris 6 r!h 1r . qf5 iEi \ It,ti s it * !S8S\$dd lr o ItI u 6 Bsiii $r !It!i rttt *s$ o r o + t it I E t nl \ i I I I , $ $ q_ i ;{o ri a ! li t : t l- "iI I t t Scan354. November 04. 2005.max nlL' ul{.pa i,! o s 3iB i,Et\ INNSrt ! ,I$ i !i-,tL iiB o GLYCOL PUMPS 15O() Lb. W.P.Oklo. City, OK 9o Uc oouEq o F trUIo trUecooo t500 r 4OO r300 r200 I too lOO0 900 800 700 600 500 400 roo 200 too 0 SYSTEM OPERATION PARAMETERS P.V. SEHIES 50 t00 t50 200 250 300 SYSIEM PRESSURE OROPS (PSIG) 2lol5 PV Strokes/Minute Ronge lO-J2 G10.r3 lssued 1 2/83 Scan355, November 04, 2005.max nL/ KIMRAY, lnc.NEEDLE VALVES 6000 Lb. W.P.Oklo. Ciry, OK l screw-\(- ,-}.- -lbndle",,frf- ffiT_*, 'Loch Nul O Ring ryPE 3O3 STAINLESS STEEL STANDARD ON ALL PUMPS EXCEPT 45015 PV PUMP Eonnel N PI VALVE ORIFICE PUMPvr r.r rvc ruMr * 2?t1 2274 22f5 cAHBON STEEL STAryDARD ON 45015 pV pUMp oNLy3/a" rgsq ,.rar,, o.ot. 1954c '9540 teSOr-JG;19548 1 962 154 2269 2274 2275 ryPE 316 STAINLESS STE€L - AVAILABLE ON SPECIAL ORDEH AND EXTRA COST r 16034 16038 Ira1 - 'r 978 227 1 2?74 2275rra" rgrrs6 rlto,, rzrs .t9tt46 roosoom 1 978 227 I 2?74 2275%a 1 978 227 t 2274 2275aru" ,n*au altu,t ** rrru 153 2270 2274 2275 :rr:: -ts55su nr.r,, ,io* Scan356, November 04, 2005.max 1 979 154 2274 22753/4" 195456 13/32" 45015 1954C6 1g54m 2269 ?274 ?275 G 10.25 lssued 7iB6 KIMRAY, lnc.GLYCOL PUMPS 1s0t) LB. W.P.Oklo. C;ty, OK CHECK VALVE BLOCKS Cage and Tellon seat darts prevenl spinning in Check Valve Blocks. Cage also acls as hold down lor removable seat. Snubber O Bing installed on stem porlion o, dart, decreases possibility ol darls sticking in caps, snubs darts befler, reduces spinning ol dart and increases pump ef,iciency. lnstalling Back-up below seats in Discharge Block allows more squeeze lo O Fing, preventing leaks. Coge Snt&r ORing Dorl lefhn Seot TeflmBdtp sttcloN cHEcK ASSEMELY pump number and service. For example: 4015 PV lor 'split discharge". To order Check Valve Blocks for Split Discharge Assemblies add an "A" to the Check Valve Body number. Example: 1194A to order the assemblies with viton O Rings add a '\r to Check Valve Assemblies number; Example: 1194AV DISCHARGE CHECK ASSEMBLY Coqe Snbber ORinq Oorl Teflm S&t Tef/m Bock-up Chect Volfr Cot) OR q lcoel Ctoch Wve Dq, O Rlng lserJ G:10.29 Bev. 2 lssued 10/94 l--n--1 Chec* Volrc aod, O Rinq (Dort) RcmNbl, *ot PART NUMBEBS FOR INDICATED PUMPS PABT NUMBERS FOR INDICATED PUMPS PART NAME OTY 1715 PV 4015 PV and 20r5 sc 9015 PV and 5015 SC 21015 P\ ud 1@r5 SC 45015 P\ and 2@15 S( CHECK VALVE BOOY 'I 1194 'Ir94 '1195 .11 96 11 97 .OT RING. SEAT 2 49't 491 'r 151 156 801 HEII,IOVABI.E SEAT 2 1152 1152 1 131 1 133 1'173 REV. BEM. SEAT 2 1947 't947 1 948 1 949 1950 "O'RING, DART 855 154 9?4 156 DART 1 307 854 118 .O"RING CAP 155 155 156 157 80r CHECK VAL\E CAP 2 1327 1327 1 199 1198 TAPPED HOLE SIZE NPT I x ,A Y, DIMENSION'A'lrches 1A 1',t Scan357, November 04, 2005.max PUMP SIZE CAGE NO, OART NO. ors OART % CAGEO RING 1715 PV 2015 SC 40't5 PV 1 941 1 940 1907 1 666 647 I735 5015 SC 9015 PV r938 1 937 1908 1 667 u7 1 736 1 933 193?1 909 1 668 153 1737 tlrd 3 KIMRAY, lnc.BALL CHECK VALVES Oklo. Cit"y, OK o 2015 SC, 1715 PV & 4015 PV SUCTION CHECK VALVE ASSEMBLY with BALL CHECK VALVE t53 O-Ring,2 Req'd. (Slolic seol on bock of block, nol shovn.) 2015 SC, 1 715 PV & 40'15 PV DISCHARGE CHECK VALVE ASSEMBLY with BALL CHECK VALVE /3OB Check Volrc Cop, 2 Req'd. /55 O-Ring, 2 Req'd. 53O O-Ring, 2 freq'd. 699 Pluq BOB qrcl Lblve Cop2 Roq'd. /55 ORing, 2 tuc'd. f/3 8o/l Check Assy.2 Roq'd. 49/ ORing,2 Req'd. 95/ DischorqeChcc* lhlve 0lock CHECK VALVE ASSEMBLIES AVAILABLE CAT.NO, TYPE 952E SUCTION951E DISCHAFGE BALL CHECK VALVES ONLY CAT,NO. TYPE 17 r 1 SUCTTON1713 DISCHARGE G:10.30 lssued 1 2/83 Check Valve Block for Split Discharge wilh Ball Check Valves are available. For easy removal of "Ball Checks" order "T" Wrench. Part Number 1827. Scan358, November 04, 2005.max t*L* t-{* *r.;# * trJffi rffi i I I oo a Co *) (U U o_ ct- d CDg o C .CU(u l'- ffi qr.{ m UJ &# I i It- J o Friday, November 04. 2005 (9).max i-c UJ{ 5C UI6 IB oo rL .gfr,o-';-lr,i;C6 ,,E'u 6 2!q o't oYrr \- J-,l= .9 ru ro BEg#Eq fr & -ir'i r.;+ I I d I I : I o Friday, November 04. 2005 (10) max f S-r!#:#f"*g fiJ *df,*lsa ffi L} ffi i,:,L Ftrul v IJ.Tffi ffi M *TLAU i5 fi$ Urtgtt*. 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B&E tr IFlr[sa :,:: :: I ffi, I i I J / / J t;lrl,li It_ Friday, November 04, 2005 (16).max nL-/ l-- OC UI {vtu& ffi oo * tE\ **,FlElr & t3w B& TM> re!* fiJ ffifiIu#rptw ffi J oa o o o o fras'ol*5 \J energy lkw* Clultis Rrrctcr Arr QLrality (loor rlinator 1625 Broadway Sirite 2000 Denver, Colorado 80202 Telr 303.389J600 Faxi 3ci,389.3680o noble energy production. inc. a suhsidiary of ncble energy inc. November 29, 2005 il.{r. Ram Seetharanr Air Pollution tlontrol Division Colorado Department of Public Health 21300 Cherry Creek Drive South Denver, CO 80246 SUBJECT: Additio*al Information lbr Noble Energy's Flyrup Production Facility - Pending Air Permit Application Dear Mr. Seetharam: Per our Nov. 21 conversations with Mr. R.K. I-Iancock, Noble Energy is subnritting the follorving supplemental intbrmation to the pending air pennit application for our Hynrp facilility locared near Parachute in Garfield Counry, Colorado. The supplemental inlbrrnation reflects both changes to some data in the existing application as rvell as the addition ol-more sources at the site. Tlre supplemental information is attacled aud is organized as follorvs: . Updated si;e-rvide emission inventory ancl process florv diagram; . Updated eniissions calculations tbr Plant ID 2 (a 1085 hp Caterpillar engine - data rnodified to retlect more appropriate ernission lactors) and Plant ID 3 (the glycol dehydrator- updated to rellect aRc\v gas anallsis and the planned addition ofa flash tank to the clehydrator); . APllNs lbr additional sources (including a J-'l' skid, amine Lrnit rvilh both a CO2 vent and a heater/reboiler vent, ard trvo addrtional Caterpillar engines that are identical to thu one described above); and . Supportiug calculations for thc adclitional sources. With regard to thc updated enrissions calculations lbr l>lant ID 2 ard 3, iVlr. l-lancock indicated llmt rve cotrld sLrtrmit the r-rpdated calculations rvithout r.ecding to complcte nerv APENs, so u,e have subrnitted only the calculations ar:d appropriate supporting data. 'I'he addition ol the amine unit is a high priority ite m lor us sirrcc rvc need it to continuc gas production in the a;'eir. so rve would appreciate your he\r in the timely processing of this application. Ilyou have any questions or nccd adtlitional irrlbrnration. pleasc contrlct rue at L-.! !r,.ti s1!t 1f L!{9_r.j1!' ! 9i.ry,..!!',ltt or a t ( 30 3 ) 3 I 9-3 649. llesards. UPDATED SITE.WIDE E1VIISSIONS AND PROCBSS FLOW DIAGRAM />6o*. o- u) fr-.c ::rc oo 6 Lu o c{N++X Lo- : ()OE 99a u)g)Y srr)c) cioE oo3 00o (,o, I sl^l_ xxE Oo I crs)C (vN VCC _ q)g)E 66A ccO LL sff& cocoE CcX coY aaTL JJ oo 9)N\Eoa c (,) oo,:o-o.x.-Eoggzg:3E; e'e.- _ {D D EEEH;;,=6X6nP€Eioo:tr\>6s =s:Bm--65HHo65Eo FEprc.cEEh>:-ggoa;sN6(s($Oi()Ntr)c0(i t-s?o Il)(o(oo? d2 0?ooo Co.{ Nqo 66(hr^ FNg)I- N €O(O(O a'lo-Ednj {9'.q oq -. c?c? \<"?ciri oooo F- o c{(\ r: = (f'- -' N o<o!E3E ONN Neqq q()Eo a O{ NOci(o ci ai6*ENNO)C)O @ -.Olr)<t+ OEqdrb:qoqo{q oq qqc!cYol \j*,.;Sqlf)lt)N- o) Nc)oon S nNr^ @ O N('n (oxld F- e qqq I"si-l ': si c)oo Oin o Gl NN N ci.e6:E g5E3 E 8 E€A E = aZd; o * 'roci +d +--N q Nc{ N 5d K E S o o.o. = c- E EE* c .o c oro,*. .= o > Oo<[ 6 O.O E O() b = !?rrr oF tlJtrl "b aE 3.?i EE, ," P1 diI e S[t EE 5 BE ;;i s.EEq+i? y rq=EEaH Egi5;o;EE-fi ef"E:EEL ooL=r\.Vcco,n b=2u== E 1E*?$grt€eB f; !$EEfifi: Sg,[8I888;" F JiY<<.,.,E t - o$Lo{oro EoEE-*1 ? -E?>rtrtr4 LY €*27--a =oi EE ]5t=>trJru = eq a'<< :'o ; .P?l3€, AEE-oC EEJoc) ];; g'ur 5 I6 le r{ I; 9 t ET es|zo9lr'<v Izo:)5 n!Cr ffi Hli a o o o : j o UPDATED CALCULATIO NS AND SUPPORTING INFOR]}IATION FOR PLANT ID 2 AND 3 o Hyrup Production FacilltY Engine Detail Sheet Source lD Number Equipment lD Source Description Engine Usage Engine Make Engine Model Serial Number Date in Service Engine Configuralion Ernission Controls ISO Rating Site Rating Fuel Healing Value Heat Rate Engine Heat Rate Permit Slatus Polenlral Enrsstbns 1085 hp Caterpillar 3516 TALE Horizontal: SCC Source Locaticn Zone: Vertical: Potential operation Previous operation Current operation Potential fuel usage Previous fuel usage Currentfuel usage Stack lD Stack Height Stack Diameter Exit Velocity Exit Temperature Volume Flow Rate 2 lnlet Compressor Waukesha 3516 TALE 4 stroke, lean burn 1085 BHP BHP 950 Btu/scf 8.14 MMBtU/hr 7500 Blu/hp-hr 8760 hr/yr hrfr hrlyr 75.04 MMscf/yr 0.00 MMscf/Yr 0.00 MMscl/yr ft in fUs 842 deg F ft3/min _ _{lglMMBtu)(g/hp-h0 (hp) (hrs/vll-.(lb/hr),-- (tpvl---.. . . Nox - m s76o 4.78 2o'95 Manufacturer lblyr Nominal Hrs missions Source Rating Operation Emission Factor 2.OO 1085 8760 4-78 20.95 Manufacturer 0.50 1085 8760 1.20 5'24 Manufacturer CO VOC SOx PMlO Forrnaldehyde Acrolein Acetaldehyde 0.000588 0.0100 0.0528 0.00514 0,00E36 1 085 1085 1085 1085 1085 0.04 0.07 3763.8 366.4 595.9 8760 0.00 0.02 AP42, Table 3.2-2 8760 0.08 0,36 AP-42,Iable 3.2-2 8760 0.43 1.BA A?'42,Table 3.2-2 0.18 AP4z,Table3.2-2 0,30 AP-42, Table3.2-2 8760 8760 Eigjflr SPaed (rlrm) CcrmpiessioD Ralio Aftercooler lnlet Ternperature ('f ) JaciGt.,Waler Outlea Tern peraluru (cr) lEnttioa SYslem Exhaust Manifol<i Combustion SYBlem TYPe Engino flating Data Engine Polrer (lrlo lan) 1200 0:t 130 2'to EIS WATER MOLED Low EMlsslol-l 190% 75% 1085 I'ld NAT GAS c20 HPG I}"IPCO 35 80 5000 .58% 542 ",/. Load bhp Btu/bhP-hr scFh* lbJlrr in. HG (abs) "F in. HG {abs) .F "BTDC .F CFt4 lbihr gibhP-hr ppfir ':._ :-.:..:.: g.rbhPhr ppm Fuel LHV of Fuel (BtdScFl Fuel Sl'ste,rl l,,,lioimum Fuel Presqure {Prig) Melhane Number at Condllions Sho$n Rated Altilude {ft) at 77cF Design TempeBture Engino Data Specilic Fuel Consumpiion (BSFC) (1) .Aji Florlr (Wei. @ 77oF 2B.S in Hg) Air Plass flow (vuet) ComPfessgl 0ut Press!re Compressor Oul TemPeralure lnlel Manifold Pressure lnlet lvlanifold TemPel"il(e (10) Timing (11) Exhaust Stack TemPerature Exhausl Gas Flo$ (Wer, @ stack lemperature' 29'7 in Hg) Exhaust Gas htass Floru (Wet) 745o 2264 10040 69,2 287 62.4 139 33 842 5977 r0437 2.0 129 -.-: 1.8 215 .:, 7540 1680 7450 64 264 47.9 138 1a 820 4388 7?56 2.6 185 8104 091 43S2 45.9 179 xo2 138 JJ 862 2681 46'r l 4.2 230 Enginc Ernissions Data Nifous oY.ides (NOx as NO2) (9) Carbon Monoxide {CO) (9) Total Hydrocarbons [fHC) (9) Non-Melhane Flydrocarbons $fdFtc) (9) (0on.15% 02) (Ccn 159d 02) {Con- 15% 02) (Corr. 15% 02) I 2,O 1.8 230 236 g/bhp-hr ppnr : I _l '-. 3.2 677 3.1 b5b ta 517 0.35sJ;6'h' pprn --" oJe 47I 0.47 43 Exhsust Dxygen (9) Lanrbda Engine l'leat Batance Data lnput €nergY LHV (1) Work Output Heat Reiection to Jacket (2) (6) Heat Rejeclion to Atrnosphere (Radialed) (4) Heat Rejection to Lube Oil (5) Tolal Heat Rsi€ction lo Exhaust (to 77'F) (2) Heal Reieclion lo Exhaust (Lt'lV to 350"F) (2) Heat Rejection to Aflerccoler (3) {7) (8) !lt 7.5 1.50 - 6.t 1.24 102239 73261 34522 23014 329s0 29325 3795 3037 00 26932 17002 18362 10751 3980 883 DM0107-03 ?; Ettr/n)in Bttr/min Btu/min Btulmin Btu/rr,in Blulmin Btuimin Btuimin -T- I .*.-::--.'" B,O 1-56 134707 45029 40G39 459 0 31337 230$4 6148 -ENGLISH- paqe 1 of 2 Engine Noise Data - at 100c/ load Noise - [iechanrcal'@ 1 m Noise - Exrausi @ i-5 m Fuel Usage Guide ....- <30 . . 30 -ot- 0.90,19 Altitude Deration Factors 1 110' 100 90 80 70 0 50 Aflercooler Heat Rejection Fdctors 130 120 1.10 100 90 80 7A 100 1i1 Dera-te iaitor / Engirre Titning vs f,lethane FllTt'-ut 80 to 6s 70 7$ 100 1-0/2S 1.0130 1.0/31 1.0i33 35 40 45 50 55 A;9O]21 0-9or22 1'0/2-3 1'Ql2/' {'0PB 0 1000 t00t- 3000 4000 5000i000 7000 0000 9000 -10000 11000 12000 ALTITUDE (FEET ABOVE $EA LEVEL) dB(A) dB(A) -..q9 -1.01n o- U]F F uJJ Z. t <{. ("F) o- til h-t- TUJ Z cra fF) 1 .37 1.d4 1.51 1 .58 'l .66 ',l .73 I .73 't '73 1 '73 1 '73 - 1-73 - 1'73 1-73 .---::::- - l j- -- 'J:-:'r.-ie r.ss'"--i.az 1.49 1.56 1.63 1.63 -1.63 1'63 1:q3* -1'F 1-63 'l'33-i.li fo '-i.1s--139i1 I sa 1.1a--1'Y -1-,!4 -.Lg-1'S- -l'54 1,!-1 l.ro t,i?- r.ar__r,s-o___M- lt!-:.lo -:tl 1:!t _144_++. 1.11--1'-41 1,01 'r.o8 1-14 t.zt tn is- 1,$ --.1-9! -!qs ..-E-5--.1-3q-- I'xs-. .1:15- . -f.qo --:t.1iq*-"i,0-q:-113:-113- .i.zs-*1.2s - r'21 -.. 1 41?5: - -y1 ^- -1.:?9--:!2 rJi.o- .-jno*jqq..ilL-:g--Uo- t.ro r-to tJ.6--ll9-,..L:19 1'16 . 1'16 1.00 1,00 1.00 r-oo -i.oo i.oo -1.q6__' 1_.-0_9. . L-0!_. 1_,0q -LqG ,i.Qq -Jp660 50 i.oo'joo- rm 1.00 1.00 1.00 1-00 1.00 1'00 1'00 1'c0 1'90 1'00 8000 9000 10000 11000 12000 ALTITUOE (FEET ABOVE SEA LEVEL) 0M0107'03 Data is intend-ed 10 be used evlth Gas ine Porformance Book Parametcrs -DM5900--00 on DM0107-03 "ENGLlSll' page ? ol 2 I t ]o 1.00 1.00 1.00 0.e8 i-e4---9,91 .--9:.q9 -0-!1- ..0-'!1---0&-- !{l g.?- ^q'9--. : -. .i*.g-. i.op- ,ng-. -,qq.-o,np*0.s.. -.0-:8-? 10-'!6. q$--9$!- -91i - 0'14 'oJi' 1.00 1.00 1.o0 r.ool.ss- o-ga o'sl - !:9-7 . -0:94 9-€-1 - " oJa- - -o-'7s " '0'L2'.:- r.oo -l.tj'o i.oo i.qo-"-.iir-.,. 9,99 9,!3 o.9g 0'9.9... -o'!2 ?:l? 0'76'-- 0'73' i.00 t,oo t,gq ., t0.--1*1-. o 9s- -0'F -991 .9,9.1 g+ . o'qr- -9:18. 9.I-5- 1.00 1.00 1,00 r.oo -r.0o-,qse ..-qgg p-.9-1-. q,p-e-- g'qq - -q,B2 g:7-g - 0'76 1.qq l,iiq iso i'oo-1.rLlqq :.:l--::: -::: +:i :ri: l:i :j: o {.oo r.o-o 1 6 - - r.00] j ,od T'.0[- -qpg -0 s'5-. -q.9?,- q,s!---g 91- - .q,"8-? q.'I9- 1.00 1.0o 1.00 r.oo rno - l.oo - 'i.'oq o.gg o'ea 0'9.0 0'87 0'Ba - 0'80- 29 ROLLED EMISSION FACTOR.S FOR 4-STROKE LEAN-BURN ENCTNESOTzble3'2-2' ttNCoNT' (scc 2-02.002-54) Pollutant Ernission Factor (tb/N4MBtu)b (tuel inprt) Enrission Factor Rating Criteria Pollutants ar:d Greenhouse Gases Noxc 90 * 1057o Load No"t <9oYo Load coc 90 - 105% Load COc <907o Load cOrd soz" TOCf MethaneE voclt PM10 (filterable)i Plvlz.5 (filterable)i PlvI Condensabld 4.08 E+00 8.47 E-01 3.17 E-01 5.57 E-01 Llo E+02 5.88 E*04 1.47 E+00 1,25 E+00 l.l8 E-01 7.71E-05 7.71E-05 9,91 E-03 B B C B A A A C C D D D Trace Organic Compounds 1,1,2,2 -T etr ach I ome th anek I .1,2-Trichlo.oethao.k 1,1-Dichloroethane 1,2,3-Trimethylbenzene 1,2,4-Trirnethylbenzene 1,2-Dichloroeihane 1,2-Dichloropropane 1,3,5-Trirnethylbenzene 1,3-Butatlienek 1,3-Dichlorop.op"n.k 2-Iulethylnaphthalenek 2,2,4-Trirncthylpcntanek Acenaphthenek <4.00 E-05 <3.18 E-05 <2.36 E-05 2.30 E-05 1.43 E-05 <2.36 E-05 <2.69 E-05 3.38 E-05 2.67E-04 <2.64E-05 3"32 E-05 2.50 E-04 1.25 E-06 E E E D C E E D D E C C C 1na Stationary Internal Combtrstion Sources 3.2-il o ' Table 3.2-2. LTNCONTROLLED EIvIISSION FACTORS FOR 4-STROKE LEAN-BURN ENGINES (Continued) Pollutant Emission Factor (lb^4MBtu)r' iftrel input) Eniission Factor Rating Acenaphthylenek Acetaldehydek'l Acroleink'l Baorao"k Benzo(b)fluoranthenek Benzo(e)pyrenek Benzo(g,h,i)perylenek Biphenylk Butane Butyr/IsobutyraldehYde Carbon Tetrachloridek Chlorobenzenek I cr,toro"tt on" lchlorofo.*k l"nor.r"u I cy.lop.ntun. lr*un" I ,,nr,ornr.n.* | ,,hr,.n" Dibrornidek I Fl,,o.rnth*r"k I rh,or.u.* I For,rold"hyark'l I iu.ttrrnotk I I lvlethllclclon.*n0",. I Methyl"ne Chloride" I n-H.^o,,.* I ln-Nonanc 5.53 E-06 8.36 E-03 5-14 E-03 4.408-04 r.66 E-07 4.15 E-07 4.r4F-}'l 2.t28-04 5.41E-04 l.0l E-M <3.67 E-05 <3.04 E-05 1.87 E-06 <2.85 E-05 6.93 E-07 2.27 E-04 r .05 E-01 3.97 E-05 <4,43 E-05 1.ll E-06 5.6'1F-06 s.2BE-A2 2.50 E-03 1.23 E-03 2.00 E-05 l,l r E-Oi t.l0 E-04 C A A A D D D D D C E E D E C C C B E C C A B C L ? C 3.2-12 EMISSION FACTOITS 7 t00 Table 3.2-2. UNCONTROLLED EIvIISSION FACTORS FOR 4-STROKE LEAN'BURN ENGINES (Continued) Pollutant Emission Factor (b/tvIMBtu)b (tuel input) Enrission Factor Rating n-0ctane n-Pentarre Naphthalenek PAHK Phenanthrenek Phenolk Prcpane P1n.rr"k l- Styrene Tetrachloroethanek Toluenek Vinyl Chloridek Xylene k 3.s1E-04 2.60 E-03 '1.44 E-05 2,698-05 1,04 E-05 2.40 E.05 4.1,98-42 L36 E-06 <2.36 E-05 2,48 E-06 4.08 E.04 r.49 E-05 1.84 E-04 U (- D D D C E D B L B u R.feren.e 7. Factors represent uncontrolled levels' For NOx, CO, and PM 10, "uncontrolled" means no combustion or add-on controls; Ilolever, the factor may include turbochargcd units. For all other pollutants, "uncontrolled" lneans no oxidation control; the clata set may include urits u,ith control techniques used for NOx control, such as PCC and SCR for lean burn engines, and PSC for rich burn engines- Factors are based on large population ofengines. Factors are for engines at all loads, except as indicated. SCC = Source Classification Code. TOC = Total Organic Conipounds. PM-10 = Particulate Matter < I0 microns (pm) aerodynamic diameter. A "(" sign in liont of a factor tleans . th.at the coresponding emission factor is based on onerhalf of the nrethod datection limit. b Emission factors rvere calculirtecl in units of (lb/MlilBtu) bascd on procedures in EPA Merhorl 19. To convert frorn (lb/MMBtu) to (lbi 106 scf), multiply by the heat content of the fuel. If the heat content is not available, use 1020 Btu/scl-. To convert l'ront (lb/MMBtu) to (lb/hp-hr) use the lbllowing equalion: lb/hp-hr = llbiMMBtul theat input, Mlt4Btir/hq 1lloperating l-lP, liltpy t Emission tests u,ith unreported load conditions were not included in the data set. d Based on 99.-s% roorrrrio, of the fuelcarbon to CO7. CO2 [ib/NINIBtu] = (3.6?X%CON)(CXDXl/h), where o/oCON = percent conversiol of fuel carbon to CO2, C : carbon ccntent of fuet by rveight (0.75), D : density of fuel, 4. I E+M lb/ I 0" scf, and 'il00 Stationary Internal Combustion Sources 3.2-13 o {,t ,l,l;p trl14frr Page: GRI-GLYCafc 1/ERSION 4.0 AGGREGATB CALCULATIONS RBPORT Case l{ante: Hyrup Production Facility eiie iri*". cilui Documer:ts\Colorado\tiyrup wiEh Netr Gas Analysis 112105^ddf DaEe: November 21, zOOs DESCRIPTION: Description: Run w/ revised gas analysj.s and add f1ash. Lank Anngal Hours of Operation: S?60.0 hours/yr EMISSIO}IS REPORTS: CONTROLTED REGENERATOR EMISSIONS Component 1bs/hr l"bs/day eons/yr Methane Ethane Propane IsobuLane n-BuLane fsopenlane n-Pentane CyclopenLane n-Hexane Cyclohexane OLher Hexanes Heptanes Methylcyclohexane Benzene Toluene Ethylbenzene Xylenes CB+ Heavies 0.3c35 o -L197 0.2c10 0.0e42 o -1263 0.0468 0.0500 0.0145 0.0347 0.0970 0.0519 o - 0607 0 - 1245 0.2881 0.3595 0.0120 0.1168 0 . 0015 7 .287 4.3].2 4.824 2.02L 3 .030 r.123 l.200 0.347 0.833 2.329 7.246 1.457 2 .989 6 .916 8.629 0,288 2.804 0.037 1 .3298 0.7870 0.8805 0.36BB 0.s530 0.2049 0.2189 0.0534 0. L520 o.4250 o -227 4 o.2658 0.5454 L.2621 t .5'l 48 0.0526 0.5117 0.0067 ToLal ToLal Hydrocarbon Total vOC Tot.al HAP Total BfEX Emi s s ions Emi ss ions Emi ss ions Emi s s ions Emissions 2 .1c.30 2 - 1530 7 -6e97 0,8112 o.7i65 51 .671- st.57l 40.072 79 -469 l_8 .635 q arqq 9.4299 7.3131 3.5531 3.4072 TINCOI.]TROLLED REGE}IERATOR EMTSSIONS Cornponent 1bs/hr 1bs/day tons/yr Inlethane Ethane Propane Isobueane n-Butane IsopenLane n-Pentane Cyclopentane n -Iiexane Cyclohezane 0.3045 0 - 1t25 0 -2173 0.o979 a -1542 0 -oiit9 o.a295 0.0951 0.3r68 7 .311 4-380 5 -2L6 2 .349 3.'102 7.'198 2 -034 0. ?09 a )9) B.OB3 1,3343 0.7994 0 _ 9520 0 .428'] 0.6'756 0.3281 o .3772 a.l.293 o.4764 t -a-752 o Ouher Hexanes HepEanes Methylcyclohexane Benzene Toluene Ethylbenzene Xylenes C8+ Heavi-es 0 .1168 0.3466 o _7572 7.2266 3.8106 0 .3684 4.A297 2 -5422 2-804 o )i o 1B - 173 29.438 9t .454 8.841 95 -952 63 .414 0 - 5118 1- 51-83 3 - 3165 5 -3724 16 .6904 1.6135 L'l -6937 11.5730 TOEAI ToEal HydrocarbonTotal vOC TOIA} HAP Total BTEX rLASH TA}IK OFF GAS Emi ssrons Emi ssions Emi ssions Emi ss ions Emi ssions 14 - 9958 1-4.8858 14 - 3985 9.5403 9 .4452 357 -259 357 .259 345 .567 228.967 226.685 65 - r-997 65 -199-1 63 - 0660 4t.7864 41 - 3700 ConponenL 1bs/hr ]bs/day tons/yr IrleLhane Ethane ProPane Isobutane n-Butane I sopentane n- Pentane Cyc)-opentane n-Hexane Cyclohexane other Hexanes Heptanes MeIhylcyc]ohexane Benzene Toluene Ethylbenzene Xylenes CB- Heavies 45.1i61 7 .Li1t 3 .4631 0.9583 1 .1255 0 _ 45s9 0 .4040 o -A'i12 0 .2330 0.2166 0.3907 0 .3 881 0 .3 s65 0.0895 0 .1565 0 - 0087 0.0530 o.2't67 la84,225 L'i2.250 83.114 23.239 27.442 10.940 9.697 0 .892 5.592 5.200 o 41.7 9 .314 8 .559 2.L47 3.998 0 .208 t.5L2 6.642 197 .8711 3a -4357 15 . L683 L )41 1 4.9297 1.9966 1 .7 696 o.1627 1.0205 0.9489 a.7t14 L.6998 1.5520 0 .3919 o.729'7 0.0380 0.2759 1.2t2)" Total Total HYdrocarbon Total voc TOLAI HAP TOEAI ETEX Emi s s ions Emi. ssions Emissions Emi ssions Ernissions 60.9956 50.9966 B -6434 0.5507 0 .3277 1463 14€3 2C'7 13 1 .918 26-l .1650 .918 267 -1654 .442 37.8582 .4sB 2 .4560 .865 1 .4355 EQUIPI,ISNT REPORTS: Condenser OutIeL TemPeraLure : Condenser Pressure: Condenser DutY: Hydrocarbon RecoverY: Produced i'Iater: VOC Control Eff-ciencY: HAP Control Ef f :ciency: 115 - 00 t2.50 6.L2e-O02 l -02 4.92 88 .40 91-50 deg. F psia l4M BTU/hr bbls/day bbls/day COND]NSER o Page: BTEX Control EfficiencY: Dissolved Hydrocarbons in llater: Component 9r-.78 ? s30.7s ms/L EmiEted Condensed Water Carbon Dioxide Nitro:gerr Methane Ethane Prapane Isobutane n-Butane Igopentarie n-.Fentane Cyclopentane n-Hexane Cyclohexane OLher Hexanes lleBEanes MeLhylcyclohexane Benzene Tofuene Ethylbenzene Xylenes CB+ Heavies 0 .318 98.00? 99 .503 99.6't?6 98.44t a1 d Qoz 85.04? B1 , B6? 62.464 58.98? 49.03t 35 -49* 2B.81tr 44.44* 1"7 .51* 16 .45* 23.49* 9.44* 5 . ZO5 2.89+ 0 .06* 99.69* 2.00t 0.50? 0 -33? l- - f o6 7.512 13.95? 18.14i' 37.54t 4L , A2e" s0.97t 63.5L2 77,A92 55.50f 82 .49q 83.55* 7 6 .5t* 90. s5* 96.742 97 .tlx 99. 94? ABSORBBR NOEE: Becaqse the Calculat.ed Absorber SLages rvas bel-ow the minimum allowed, GRI*GLYCa1C has set the number of Absorber stages to 1.25 and has ealculaEed a re'rised Dry Gas Devr Point - CalculaEed Absorber SLages : CaLculated DrY Gas DerY Point: 1.25 5 - 45 1bs . H2O/I.'il\,lSCF ?emperaEure: 110.0 deg. F Pressure: 900-0 Psig Dry Gas Flow RaLe : 22. o0oo MMScF/day Glycol l,osses 'rJith Dry Gas: 0'4855 lb/hr i{ei Gas water conuent: saEuraEed Calculaied I{et Gas Water Content : 84 ' 81 Ibs - H2O/MMSCF Specified lean Glycol Recirc. RaEio: 3.00 galllb H2O Component Remaining Absorbed in Dry Gas in GJ-YcoI $Iater Carbon Dio:<ide Ni t rogen Methane Ethane Propane Isobutane n-Butane IsopenEane n-Pentane Cyclopentane n-Hex-ane Cyclohe:<ane 7 .59* 99.87"6 99.98? 99.98? 99.95? 99.922 99.90"6 99.872 99. BB? 99,B4z 99.342 99.76"6 98.942 92 - 472 0 .19? 0 .02'6 0 -02"6 0.05? 0.08* 0.108 0-13? 0 .tzz 0.162 0.65? 0.242 1.06? o Page: oth,er HexaRes Ilepba,nes Methylcye'1ohe):aile BdRzene Tofuene Ethylbenzene Xylenes C8-r Heavies Page: 0. L9& o .42* 1.1lt 8.s9* 11. ?88 a4.5:tZ L9. 8?? 1. 53? 99 .A)-* 99 . sat 98 .89% 91 - 4lt 88.22* 85.43ts B0 .13t 98 -47t FIJASH TANK Flash Control: Vented to atmosphere Iilash ?emperature: 100.C deg. F Flash Pressure: 40.C Psi.g ComponenL teft in Removed ir:Glyco1 Flash Gas Water Carbon Dioxide NiErogen MeLhane Ethane Propane Isobutane n-Butane Isopentane n-Pentane Cyclopentane n-He):ane Cyclohexane 0ther Hexanes Heptanes Methylcyclohexane Benzene Toluene EEhylbenzene Xylenes C8+ Hear.ies 99 .B'lZ I -01% 0 .53t 0 .672 2.482 5.9r.8 9 .1Bt 1_2 .052 14 .33? 77 .57* 44.522 a o 119 6)" -9896 23.49* 4't -18* 69.L42 93.542 96.L42 97 .932 9B .66* 91 .5Bg 0 - r.3% 90- 93? 99 -37* 99, 33t 97.522 94 .092 90.822 8?.95? 85 .672 82 .432 55 .48?'t0.782 38.02? 76.5L8 52 .622 30.86? 6 .462 3. B6? 2.O'tz t.342 8.422 REGENERATOR No Stripping cas used in regenerator. Cornponent Remaining in Glycol DisEi 1 I ed C,rrerhead I{ater Carbon Dio>:ide Ni trogen I,lethane Ethane Propane Isobutane n-Butane fsopentane n- Pentane 1o iog 0.00?r 0.00* 0,00t 0 .00% 0 .00% 0 .00? 0 ,00t 1 .'t 52 L.602 70.51e 100.00? 100. 00&r 100.00t 100.00? 100.00t 100. 00? 100.002 98.242 98 .402 o o Page: Cyclopentane n-Hexane Cyclohexane Other Hexanes fieptanes I'{ethylcyclohexane Benzene Toluene Ethylbenzene Xylenes C8+ Heavies 0 .95*: 1-14+ 4 -64"6 2.59"i O.82B s.23* 5.2'1"6 I .14? r-0-s5? 13 - 034 72 -25"6 99. 05* 98.86* 95 " 36qr 97.4!* 99.1BB 94 -77* 94.73+ 91.86t 89 .45* 86.972 87 -75+ STREAM REPORTS: WET GAS STREAIU Temperature: 110.00 deg, rPressure: 914,70 psia FIow RaLe; 9.19e+005 scfh Component Conc. Loading(vol?) (1b/hr) Water Carbon Dioxide Nit.rogen Met.hane ELh.ane propane Isobutane n-Butane Isopentane n-Pentane Cyclopentane n-Hexane Cyclohexane Other llexanes Heptanes l,lethylcyclohexane Benzene Toluene Et.hylbenzene Xylenes CB+ Heavies \.79e- 001 7 .79e+001 6.72e+O00 7.15e+003 7 .79e-O02 5.28e+001 8-41e+001 3.27e+004 5.93e+000 4 - 31e+003 1.74e+000 3 .40e- 001 3 .51e- 001 1 - 23e- 001 9.98e-002 4 , 99e- 003 4 -29e- 002 2.3Oe-OO2 7.'79e-O02 5.59e-002 3 .'7 9e-O02 7-99e-003 1 .50e- 002 9-98e-004 7 - 99e-003 4 .29e- O02 1 .85e+003 4 -79e+0O2 5 .08e+002 2.14e+OO2 1 - 74e+002 I .47e+000 I .95e+00L 4 .68e+001- 1 -62e+0O2 1 .35e+002 9 - 02e+001 1 - 5Le+001 3 .34e+001 2 .57e+000 2 .05e+001 !.77e+0O2 Total Components 1C0.00 4.83e+004 DRY GAS STREATI Temperatul'e: Pressure: FIo'rJ P.ate: 110.00 deg. F 91"4 - 70 psia 9 -17e+005 scfh Component Cor.c. Loadi.ng(vo1?) (1blhr) o Page: Wat,er Carbon Dioxide Nitrogen Me'.thane EEhane Propane fsobulane n-Butane Isopentane n-Perrtane Cyelopentane n-He):ane Cyclohe>:ane 0Eher Hexanes Hepbanes Mebhylcyclohexane Benzene Toluene ELhyl-banzene Xylenes C8+ Heavies 1.36e-002 6.72e+000 7.goe-0O2 B .43e+001 5.93e+000 1 .74e+000 3 - 41e-001 3 . 62e- 001 1 .23e- 001 9. 99e- 002 4 . 9?e'003 4.29e-A02 2,28e-0Az 7.'?9e-OO2 5.5Be- 002 3.76e-002 7 . 31e- 003'J-.32e-002 B. 54e* 004 5.4]-e-003 4 .24e-Oaz 5 .91e+000 ? .1-5e+003 5 . 2 8e+O0l- 3 - 2?e+004 4 .31e+003 1 - 85e+003 4 .7 8e+002 5 - 0Be+O02 2 .14e+002 1 .74er002 8.42e+000 8.93e+001 4.63e+001 1 - 62e+002 l- .35e+002 B .92e+001 1 - 38e+001 2 .95e+001 2 " 1ge+000 1.54e+001 7-.74e+A02 loEaI qomponents 100,00 4,82e+004 LEAN GLYCOL STREAM Temperature: 110.00 deg. F Flow RaEe: 3.56e+000 gpm Component Conc. Loading(wt?) (1blhr) TEG IrIaLer Carbon Dio>:ide NiLrogen l{ethane Echane Propane Isobutane n-Butane Isopentane n-Pentane Cyclopentane n-Hexane CycJ.ohexane Other Hexanes Hept.anes t'lethyI cyclohe>:ane Benzene Toluene Ethylbenzene Xylenes CB+ Heavies 9.84e+001 1.50e+000 6.91e-011 4 .66e- O1.4 I . 72e- 018 4. B0e-008 2 - 83e- 009 7 - 11e-010 8.07e-010 5 . 57e- 005 6. B6e-005 l- .41e-005 5.45e-005 8 . l-7e- 004 1 , 55e- 004 1,.42e-004 2 . 08e- 003 3 .40e*003 1.58e-002 2.17e-o03 3.02e-002 l.B4e-002 1 " 97e+003 3.01e+001 1.39e-009 9 - 35e-013 1 . ?5e-016 9 - 63e-00? 5.58e-008 l- - 43e*008 1 .62e-008 1 .34e-003 l- . f 8e-003 2. B3e-004 1 - 09e-003 1.64e-002 3.1Ce-003 2.85e-003 4 - 18e-002 5.81e-002 3.38e-001 4.34e-0Q2 6 - 05e- 001 3 .59e-001 Total Components 100.00 2.01e+003 Page: R]CH GLYCOL AND PUI,{P G!{S STREA.I'I femperature: 1,1-0. 00 deg- F Pressure: 914 .70 Psia F1o!, Rate: 3.92e+000 gpn I{OTE: St.ream has more than one Component phase - Conc- Loading(utt) (1b/hri TEG lilat,er Carbon Dioxide NiErogen I,lethane ELhane Propane Isobutane n-Butane Isopentane n-PenLane Cyclopentane n-He>:ane Cyclohexane othe:: Hexanes !ieptanes Methylcyclohexane BenzeRe ?oluene Ethylbenzene Xylenes C8+ Heavies 9 .07e+001 4.70er000 1 - 04e+000 3.42e-003 2.09e+000 3 .3Be- 001 1 . 69e- 001 4,90e-002 5 - 88e- 002 2.45e-002 l" - 9?e+003 1.02e+002 2.2ie+jO), 7.44e-OO2 4 - 55e+001 7 -36e+000 3 .6Ee+000 1 .07e+000 1.26e+000 5 .32e-001 2.25e-A02 4.90e-001 3.08e-003 6,7Ce-002 1.5],e-002 3.29e-001 2.62e-002 5.7Ce-001 2.35e-002 5.11e-001 3 - 39e-002 5 - 31e- 002 5 - 35e- 002 1.98e-001 1. 93e-002 2 - 15e- 001 L.51e-001- 7 -3€e-001 1.1€e+000 1 . 3 6e+0O0 4.31e+O00 4.21e-001 4 - ?1e+0OO 3 .29e+000 Total Components FLASH TANK OTF GAS STREAM 100.0O 2.L6e+003 Temperature: 100.00 deg. F Pressure: 54.70 PsiaFIot, Rate: 1.40e-003 scf h ComponenL Conc. Loading(vo1?) (1b/hr) FIater Carbon Dioxide Nitrogen Methane EEhane Propane Isobutane n-Butane Isopentane n-Pentane CyclopenLane n-Hexane Cyclohexane Other Hexanes HepE.anes tlethylcyclohexanegenzene 2. O0e-001 1 ,27e+001- 7.17e*O02 7.65e+001 6 .48e+0o0 2 .13e+000 4 . 52e- 001 5 .25e - 001 1.72e-001 1 .52e-0O1 1 .44e-002 7 -34e-0O2 6.99e-002 1 .2le-Co1 1 - 05e- 001 1.3-:.e-001 2.06e+001 7 .4Oe-0O2 4 .52e+001 ?,18e+000 3 .46e+000 9.58e-001 1 - f -ie+0O0 4 - 56e-001 4 . 04e -0O1 3.72e-0O2 2 - 33e-001 2 .1ie-001 3 - 9le-001 3 - Bfie-001 9.86e-002 3 - 5ie-001 3 . 11e- 002 8 -95e-OOZ o Toluene 4 - 91e-002 uehylbenaene 2 .22e-003 Xylenes 1.61e-002 C8+ Heavies 4.41€-O02 Page: l- - 6re*001- 8.69e-003 6.30e-002 2 -7'ie-OO1- Tota1 Components FI,ASH TA}iK GI#COL STREAM 100.00 8 .1te+001 Temperature: 100.00 deg. F Flort Rate: 3.74e+000 gpm Component Conc. toading (vrL? ) ( Ib/hr) TEG Water Carbon Dioxide Nitrogen Methane ELhane Pro. pane trsobutane n-Bubane Isopentane n-Pentane CycloPentane n-Hexane Cyelohexane oEher Hexanes Heptanes ilethylcyclohexane Benzene Toluene ELhylbenzene Xylenes CB+ Heavies 9 .42e+001 4 . B7e+000 9 . B2e-002 2 -25e-0AS 1.45e-002 I . ?2e-003 1 .04e- 002 4 . 57e- 003 7.37e-.003 3 . 64e- 003 4 - 11e- 003 1.42e-003 4 . 59e- 003 1.69e-002 5 . 73e- 003 I.67e-402 3 .82e-002 5.18e-002 1. 98e-001 L -97e-OO2 2.22e-Ola 1.44e-001 1 .9?e+003 L . OZe+AO2 2 - 0€e+000 4 -72e-004 3 .05e-001 1 .8-ee-001" 2 . 1?e- 001 9 .79e-002 1 ,54e-001 '7 .62e-0O2 B .51e-002 2 .9te-002 9 -52e*QO2 3 . 5-1e- 001 1.20e-001 3.49e-001 7 .99e-001 1 .29e+000 4 ,19e+000 4 .12e-001 4.64e+000 3 - 01e+000 ToEaI ComPonents REGE}IERATOR OI/ER}IEADS STREAM 100.00 2-09e+003 Temperature: 2].2.O0 deg' F Pressure: 14. ?0 Psia FLovr Rate: I.50e+003 scfh Component Conc. Loading(vol?) (Ib/hr) lniater Carbon Dioxide Nitrogen Metlane Ethane Propane Isobutane n-Butane Isopentane n - Pentane 9 .49e+001 1.11e+000 4.00e-004 4 .51e-001 1 .44e-001 1 , 17e- 001 4 . 00e- 002 5.30e-002 2 .46e-OO2 2.79e-402 ? .20e+001 2 .06e+000 4.'l2e-0O4 3 .05e-001 1 - 83e-001- 2 .1re-001 9.7 -qe-0OZ l- . 54e- 001 '7 -49e-002 8.4ie-002 a Page: cyclopenEar1e n-Ilexane Clrclohexane Otber }lexanes Itreptsanes Methylcyclohexane Benaene Toluene ELhylbenzene Xylenes C8+ Heavies 1.00e-O02 2.62e-0a2 9 - 50e- 002 3 -22e-O02 B-2Le-002 1 - 83e- 001 3 . ?3e- 001 9 .82e- 001 'B -24e-OA2 9 - O3e-001 3 - 6Be- 001 2 - 95e-002 9 .5le*002 3 -3?e-OO1 1.1?e-001 3 -4?e-001 7 .5?e-001 1 - 23e+000 3 - B1e+000 3 .68e-001 4.04e+000 2.54e+000 Total Components CONDENSER VENT GAS STRE,AM 100 .00 I .89e+001 Iemperature: Pressure: Flor,r Rat.er 115.00 deg. F 12.50 psia 4 .02e+001 scfh Component Conc- Loading (wo1? ) (lb/hr) Water Carbon Dioxide Itrit.rogen Methane Ethane ProPane lsobuEaue n-Eutatle Isopentane n-Pentane Cyclopentane n*He:<ane Cyclohexane OLher Hexanes HepL.anes ItleLhylcyclohe:<ane Benzene Toluene Ethylbenzene Xylenes C8+ Hea'/ies 1.19e+00L 4.33e+001 1.58e-002 1.79e+001 5.54e+000 4 - 31e+000 L.3?e+000 2.05e+000 6.12e-001 6-54e-001 1.95e-001 3.80e-001 1.09e+000 5 - 69e-001 5 -72e-00L l-.20e+000 3.48e+000 3.59e+000 1 .07e-001 l-.04e+000 8 . 45e- 003 2.2"!e-AQl 2 .02e+000 4 -70e-004 3 -04e-001 1 - 80e-001 2 .01e- 001 8.42e-0A2 l" . 26e- 001 4 . 6B.e- 002 5 .00e-002 1 - 45e-O02 3.4?e-002 9 - 70e- 002 5 .19e-0o2 6 .0?e-002 1 .25e-001 2 .8Be- 001 3 .60e- 001 I -20e-002 1 .1?e-O01, 1 .52e-003 ToLal Components CONDENSER FROfUCED WATfR STREF.M 100,00 4.40e+000 Temperature: Flow Rate: 115-00 deg. E 1 -43e-001 gpm Component Conc- Loading (wt?; ) (1b/hr )(ppm) Iilarer Carbon Dio:<ide Nitroqen Methane Ethane 9.99e+001 7.1?e+001 3.39e-OO2 2 -43e-002 1.99e-007 1.4Je-OO't 2.51e-004 1-80e-00.1 1.72e- 004 1-2le-004 999130. 339. 0. 3. 2- I EMPACT ANALYTICAL SYSTEMS, INC 365 SOUTH MAIN STREET BRIGHTON, CO 8060I (303) 637-0"'so EXTENDED NATURAL GAS ANALYSIS fDHA) PROJECT l'lo. : 0511038 COMFANYNAME : N0BLTENERGY AGCOUNTNO.: PRODUCER : LEASENO. : NAMBDESCRIP: HYRUPPRODUCTION*!FIELD DATA'' SAMPLED BY: M. LAWRENCE SAMPLE PRES.: SAMPTETEMP. COMTdENTS : t,loLE % 0..)00 0.c00 ANALYSIS NO. : O2 ANALYSISDATE: NOVEMDERT,2()O5 SAMPLEDATE : NOVEMBER 1,2005 TO: CYLINDER NO. : 89 COMFONENT TELrufrr - HYDRCGEN OXYGEN/ARGON N1TROGEN co2 METHANE ETHANE PROPANE I.BUTANE N-BUTANE I"PENTANE N.PENTANE HEMNES PLUS TOTALS DIEXCOiIII'ONENT|IlIOLT% \ITI% BENZENE O.OO8 0.032 LO\Y NET DRY REAL; ETHYLBENZENE O.OO1 O.OO7 NETWETREAL:TOLUENE 0.015 O.O7O HIGH GROSS DRY REAL :XYLEI{ES O.OO8 0,043 GROSS WET REAL: TOTAL BTEX 0.032 0.152 NET DRY REAL : GROSS DRY REAL: (CILC: 5PA $1D 2la5 & 1'P.17 (.ijt1.a96 & 60 , , DTI.4 (D ET.l ILE D I I'' D ROCA RBO;I AI*,4/'.''SIJ, NJ I 9' J) RELATIVE DENSIry (AlR=1 ): COMPRESSIBILITY FACTOR : : tSTtrl D6730 TTlIS DATA ff/IS BEEil ACS|JIRED THROUGIT APPI,ICATION OF CUP.RENTSTATE-OF-ME.IRT )NNLWICALTECIINIQIJES. THE US9. OF THIS tNFO$l.rTION IS TtlE RESP2)islBUlt OFflrE USER. EilP,tCT )NALr'flC.11Sl'STElrtS. SSSUIIES uO RF.SPONSIBUN'FOR ACCI;MCf OF TilIi REPORTED TNFORT/,J?7O.VAIOA 'NY CO,\'SCQ{JENCES OF I'I'S SPPUCNToN. 0.000 0.0b0 0.078 0,1106.732 14.866 u.271 67,829 MASS %--6.0oo 0.000 0.361 B'r-u@ AMBIENT TEMP,: GRAVITY : GPM@j*GPM@j,," 5,936 8.356 1.739 3.U7 0.341 0.9940.362 {.056 0.123 0.448 0.100 L5840 o.4181 0.11 '13 0.1 139 0.0448 0.0361 1.5877 0,4792 0.1 116 0.1142 0.0449 0.03620,318 1.533 0"1311 0.1311100.000 ##### 2.4993 2.5049 t4.696 949.58 Aef 933.03 /scf 1050.62 /scf 1032.31 Acf 18038 /lb 1 9958 /th 14,73 951.77 /scf 935.22 lscl 1053.05 /scf 1034.74 lscl 1 8080 ilb 20004 ltb 0.6894 0.99736 o Eh{PACT ANALYTICAL SYSTEMS, INC 365.SOU H }VIAIN STREJT BRIOHTON, CO 8060I (303i 637-0150 e & P /Qlycal. lnfannatio PROJECTNO. : D5I1O38 cdl,lPnNv NRtrlE , IioBLE ENERGY ACCOUNTNO. : PRODUCER : LEASE NO. : NAMEDESCRIP: HYRUPPRODUCTION -*FIELD DATA"' SAMPLED BY: M. LAWREI,ICE SAMPLE PRES. : ANALYSISNO,. 02 ANALYSIS DATE: NOVEIVIBER ?,200, SAMPLEDATE : NOVEMBER1,2005 TO: CYLINDER NO: 89 AMBIENTTEMP..: GRAVITY : SAMPLE TEMP. : 0.000 0.000 0.000 '3:ii3 -htptitlL'tl.1Iq"67.829 llt s.ss6 I#"3.847 I c.ee4 i,1.056 { 0'448 I $ 0_361 0.019 0.187 0.096 0.340 0.280 c.185 c.000 0.032 0.070 0.007 0,043 0273 109.000 0.000 COMMENTS ,. Componenet Heliurn Hydrogen Methanol Carbon Dioxida Nitrogen Methane Ethane Propane lsobutane n-Bulane lsopentane n-PenEne Cyclopentane n-Hexane Cyclohexane Other Hexanes Heptanes Methycyclohexane 2,2,4 Trimethylpentane Benzene Toluene Elhylbenzene Xylenes C8+ Haavies Silbtotal Oxygen Tolal Mole o/p 0.000 0.000 0.000 6.732 0.078 u.271 5.936 1.739 0.341 0.362 0.'123 0.,l00 0.00s 0.043 0.023 0.074 0.056 0.038 0.000 0.008 0.015 0.001 0.008 0.043 100.000 0.000 100.000 EMPACT ANALYTICAL SYSTEMS, INC 365 SOUTH I\IAIN STREET BRIGHTON, CO 80601 (303) 637-0150 EXTENDEDNATURAI-GM PROJECTNO. : COMPANY NAME: COMFONENT 0511t)38 NOBIJ ENf,RGY PIANO # P1 P2 9? l4 P4 l5 t5 P5 lb N5 I6 l6 t6 P6 t7 N6 t7 17 A6 t7 Ub t7 U N7 t7 N7 N7 lt N7 t8 P7 N7 t!/ t8 N7 l8 t8 t8 N8 IB N8 A7 t8 t8 t8 IB tg N8 IB ANALYSIS NO. : ANALYSIS DATE: OL NOVEMBER 7,2t)O5 HELIUM HYDRCGEN O}TGEN/ARGON NITROGEN co2 METI.TANE ETHANE PROPANE I.BUTANE NJBUTANE 2,2 DIMETHYLPROPANE I.PENTANE N.PENTANE A? DIMETHYLBUTANE CYCLOPENTANE 2,3 DIMETHYLBUTANE 2.METHYLPENTANE 3 METHYLPENTANE N-HEXANE 2,2.DIMETHYLPENTANE MEIflYLCYCLOPENTANE 2,4 DIMETHYLPENTANE 2,2,3 TRIMETHYLBUT-AN E BENZENE 3,3 DIMETHYLPENTANE CYCLOHEXANE 2 METHYLHEXANE 2,3 DIMETHYLPENTANE 1,1 DIMETHYLCYCLOPENTANE 3 METHYLHEXANE 1,C 3 DIfuIETHYLCYCLOPENTANE 1.T 3 DIMETHYLCYCLOPENTANE 3 ETHYLPENTANE ,I,T 2 DIMETHYLCYCLOPENTANE 2,2,4.TRI METHYLPE I.ITANE N-HEPTANE 1,C 2 DIMETHYLCYCLOPENTANE METHYLCYCLOHEXANE 2,2.DIMETHYLHEXANE ETHYLCYCLOPENTANE 2,5.DIMETHYLHEXANE 2,2.3.-RI METHYLPEI,ITANE 2,4.DIMETHYLHEXANE 1 C.2T,4-TRIMETHYLCYCLOPENTANE 3,3.DIMETHYLHEXANE 1 T,2C.3.TRIMETHYLCYCLOPENTANE TOLUENE 2.MEI HYL. 3.ETHYL PENTAI'.] E 2.METHYLHEPTANE 4-METHYLHEPTANE 3.M ET HYL.3- ETHYL P EI.JTA'',]E 3,4.0I\IETHYLHEXANE s-IvIETHYLHEPTANE 1 C.2T.3-TRIMETHYLCYCLCP ENTAIIE 3.ETHYLHEXANE MOLE % 0.000 0.000 0.000 0.078 6.732 8i,271 5.936 1.739 0.34i 0.362 0.003 0.120 0.1 00 0.0M 0.005 0.007 0.032 0.017 0.043 0.001 0.0.18 0-002 0.000 0.008 0.001 0"023 0.008 0.002 0.002 0.008 0.003 0.003 0.001 0.004 0.000 0.019 0.001 0.038 0.001 0.001 0.00f 0.000 0.001 0.001 0.001 0.001 0.0'15 0.001 0.004 0.001 0.000 0.000 0.002 0.005 0.000 MASS % 0.000 0.000 0.000 0.110 14.866 67.829 8.956 3.817 0.994 1,056 0.012 0.436 0.361 0.017 0,01s 0.032 0.140 0.074 0.187 0^006 0.077 0.0'10 0.002 0.o32 0.003 0.096 0.042 0.012 0.009 0.038 0.015 0.0'13 0.003 0.020 0.001 0.0s6 0.004 0.1 66 0.008 0.007 0.005 0.001 0.005 0 00s 0.0c3 0.0c5 0.070 0.0c7 o.420 0.007 0.0c2 0,0G1 0.013 0.027 0.0c2 1.5840 0.4781 0.1 113 0.1 1 39 0.0010 0.0438 0.0361 0,0017 0.0015 0.o029 0.0132 0.0069 0.0176 0.0005 0.0064 0.0009 0.0000 0.0022 0.0005 0.0078 0.0037 0.0009 0.0008 0.0037 0.0012 0.0012 0.0005 0.0016 0.0000 0.0087 0.0004 0.0152 0.0005 0.0004 0.000s 0.0000 0.0005 0.0005 0.0005 0.0005 0.0050 0.0005 0.0021 0-000s 0.0000 0.0000 0.0010 0.0023 0.0000 't.5877 o.4792 0.11 16 o.1142 0.0010 0.0439 0.0362 0.0017 0.00't5 0.0029 0.0'132 0.0069 0-0176 0.0005 0.0064 0.0009 0.0000 o.0022 0.0005 0.0078 0.0037 0.0009 0.0008 0.0037 0.0012 0.0012 0.0005 0_0016 0.0000 0.0087 0.0001 0.01s2 0.0005 0.0001 0.0005 0.0000 0.0005 0.0005 0.0005 0.0005 0.0050 0.0005 0.0021 0.0005 0.0000 0,0000 0 00.t0 0.0023 0 0000 GPM !*_ GPMf o 1 T,4.0 tM ETHYLC'TC LOH EXANE 1,1 -DIMETHYLEYCLOHEXANE 2,2,}:RIMETHYLHSGNE 3C'E IHYLMETFIYLCYCLOPENTANE 3I-ET|IYLMETHYLCYCLOPENTANE 2T.E'THYLMETHY LCYCLOP ENTAN! 2,2.4.TR1 METHYLHEXANE N:OCTANE l,l,4.TRIMETHYLCYCLOHEXANE 2,4.DIMETHYLHEPTANE 2,2.DIMEThIYLHEPTANE ETHYLCYCLOHEXANE 1 CI3C,SJRltvl ETHYLCYCLOHEXAN E ETHYLBENZENE l,3.DIMETHYLBENZENE (M-XYLENE) l,4.DIMETHYLBENZENE {P-XYLENE) 4-ETFffLHEPTANE 2.METHYLOCTANE }METHYLOCTANE l,z.DIMETHYLBENZENE (O-XYLENE) UNKNOWN OCTANES N.NONANE 2;&DIMfTHYLOCTAI,.IE 2,$PIMETHYLOCTANE N"PROPYLBENZENE 1.3.M ETHYLETHYLBENZENE T"BUryLBENZENE UNKNOWN NONANES N8 N8 t9 N8 N8 NB t9 P8 Il9 t9 t9 N9 NS AB A8 A8 ts t9 l9 AB U8 P9 t.t0 110 A9 A9 A10 U9 P10 P11 0.002 0.001 0.000 0.000 0.000 0.000 0.001 0.007 0.002 0.001 0.001 0.001 0.001 0.001 0.005 0.002 0.001 0.001 0.001 0.00'l 0.001 0.002 0.000 0.000 0.000 0.000 0-000 0.000 0.001 0.000 0.0i3 0.004 0.001 0.002 0.002 0.002 0_009 0-039 0.0i2 0.007 0.005 0.005 o,004 0.007 0.028 0.0i0 0.004 0,007 0.006 0.005 0.005 0.01.1 0.003 0.003 0.003 0.003 0-002 0.003 0.004 0.002 100.000 0.0009 0.0005 0.0000 0.0000 0_o000 0.0000 0.0006 0.0036 0.0010 0.0006 0.0006 0.0005 0.0005 0.0004 o_0019 0,0008 0.o006 0.0006 0.o006 0.0004 0.0005 0.0011 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0006 0.0000 2.4993 0.0003 0.0005 0.0001 0.000, 0.0001 0.0001 0.0005 0.0035 0.0010 0.000i 0.0006 0.000s 0.0005 0.0004 0.001s 0.0003 0.0006 0.0005 0.0000 0.0004 0.0005 0.001'l 0.0000 0.0000 0.0000 0.0000 0.000D 0.0000 0:0006 __-_q!99!. 2.5049 N-DECANE N-UNDECANE APEN FORMS FOR ADDITIONAI, SOURCES 1i Ll al.-t ,11 -.vt4il 'Jl r;l =l.fl 1;l -le.lI.t ,l al 1l :'l5 =l E '= q o 'n ,/l as.J c0 pc ?_> A> clb l<6 t>_El&- I O.iItt ilZu lr-,t4Elzgto'* IL!?l'-.2 q lA;= I ^ boa l7a 3 t3 let':t-ITt6l! ll 6 ll s E=llE =ll Ee 1:\.av c 3 I 1' L -6>>2ll , Cc.C o <)a =4 N J tr9 1 -= r !, co6a==,.trl dn*g !it, EJ Eo6 q) f.EE'^€.l =e;.\*u >'l:.o iiz-H !Es:S- Li .Y E F 6<=i rl;.',8I'9 o.b i!1o q *?i -r*!E:.!Z*QtsZO AtrDtrtrtr rt co odo.9 =As< E-iil =4. ,6 o5l)5 6c AU ,=o=F.c 6c,no a2 iiL P- ,9x '1i= i + P.6 * h j LL F o 'J r(J F U ? 5t: l<Irll oN 6.. at A - t, c N oE ;aa IJ C3 I ) o o c,Eb ,J,o o Ed oI -,oON o .=! o !) p: U:] =d 3= L t_" lcl(,3 !l c_!o ota IEEI L^*r .oo' Z, ie zr! 9; 96.=>o q< =i = ==o3.9 6u? .:x.z:!;ns E<!{o d vE36r'; ^ = a)U tr ov o6Lo Z =LO-d?sd -) =) a o: ro ah oz B e) 2 U g 1i-t 5 a 6q .2^ q d 5 d A E t) 4 o L t a z9oF-o YF I!,{ a.l o" J ul) =t,; >A ,a2Zi- qU <=vFaY),- Z=O ,tt -Gl14a z riF lz-aY,fr <rSrl,. 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IEl@ lotalqod (n o a 6/- c.) rJn ooo.l N l^lzldIElel-lol9 l6liil'dl=Iot>t:let;Io l?,lo lp.l'oloIN l5 1"2I] Ec0oJ oI 6 .gra c,) c) & Q ,io a. cJ d L-l c3 () () t- o ,. o TJ< 6q) a o roa d U oZ oE o 6 o =oU o o N ae- =E 6N :cs e = ,a .2 o c-gg 6p o.uG'E> trt g =-. I )() EI ,ii i a= ,;v) 4 t r-' T1 \a \1) \o ,o o trEoi ficn Llr] GItI* Nv q N IA o ta: o.:,FcE= =0op .9Ead 6coc.r iitrt .ZoEl:?- .o HE 5.1 coE,E6' +.eulo -t4gtr EaU z z *r'E- ii U o'(, 0) 6' o o O 0 x a oo .? oa glu 2= :z .9 -U O O ca a.l C o r-- a= vc}r O! \5c\ fr!<) car *,d (ir fi fa, f.tc)ct c.)\o eri {J U rn IJ qi I cd o eo qg-d =(n I! l>. u i I I I I I I I I I I I I I I-t€tO\ldl,;lcolFl t'l *ol o3IE > |r',zt.2>tE7t =zlu E.. cJ o=EOO^ '-l aoCqsiia4 A. d to!o /. C) aZ d tr o O=) E2L,tu no tIJ C) troz ZI A:rAE trEELUcacFo?z';<flt-e -d, IL -J3IJ9 - a.6 TE N,g LUJ EO F N,o TL I,UN T,EuI *.l-E =N,io )o SUPPORTING CALCULATIONS FOR ADDITIONAL SOURCES Hyrup Productipn Facility Heater / Boiler Detail Sheei Source lD Number Equiprnent lD Source Description Equiprnent Valve Pump Seals Others Connectors Flanges Open-ended lines JT FUG JT FUG Fugitive Emissions kom J-T Skid Service Count Gas Light Oil Gas Light Oil Gas Light Oil Gas Lighl Oil Gas Lighl Oil Gas Light Oil TOC Emis. Factor (lb/hr/source) % VOC 0.00992 8.24Yo 0.0055 100o/o 0.00529 8.24D/. 0.02866 100% 0,0194 8.24% 0,0165 10Ao/, 0.00044 8.24e/o 0.000463 100Yo 0.00086 8.240/o 0.000243 fio% 0.00441 B.24Yo 0.00309 100o/o TOTAL voc voc (lb/hr) (tons/year) 0.049 4.224 0.000 0.057 0.0'16 0.083 0.000 0.000 0.458 0.003 0.023 0.002 0.005 bU 40 0 2 10 5 80 50 30 20 0 0 4.215 0.964 0.000 0.000 0.251 0.000 0.070 0.361 0.000 0.013 0.101 0.000 0.009 0.021 0,000 0.000 0.000 2.006o TABLE 2-4. OlL AND GAS PRODUCT]ON OPERATIONS AVERAGE EMTSSION FACTORS (kglhrlsource) Emission FacLor Eqqipment Type Servicea (kg/hr/ source) b Valves Purnp seal s ot.hersc Connectors Flanges Open-ended lines Gas Heavy oil T'ight oi1 water/oi1 Gas Heavy Oil Light Oi1 }farer/oi1 Lrd - Heavy oil Light oil warer/oi1 ud5 Heavy OiI Light. oi1water/oiI ud5 Heavy OiI LighL Oil water/oi1 Gas Heav-y oil Light oi1 I(traLer/Oi1 4.58-03 8 .48- 05 2-5E-03 9.88-05 2-48-03 NA 1 .38-02 2.48-05 8.88-03 3.28-05 7-58-03 t.4E-02 2 -CE-04 7.58-06 2,tE-04 1- .18- 04 3-9E-04 3 .9E- 07 1.1E-04 2.9E,-06 2.0E-03 I .48- 04 t_ .48- 03 2-5E-04 awater/OiI emission factors apply to water streams in oi1 service vrith a waLer content greater than 50t, from the point. of origin t.o the point where the water content reaches 99?. For water sLreams wiLh a water content greater than 99?, the emission rate is considered negligible-bThese iactors are tor toeal organic compound emission rates (including non-VOC's such as methane and ethane) and apply to light crude, heawy crude, gas plant, gas prcduction, and of f shore f ac:Iities. rrNArr indicaues that noL enough data were available to develop the indj.cated emission factor.cThe Hother" equipmenL L)npe was derived from compressors, diaphrams, drains, dump arms, haLches, insLruments, meEers, pressure relief val-ves, polished rods, relief valves, and vents. This "other" equipment Eype should be applied for any equipmenl Lype other than connectors, flanges, open-ended lines, pumps, or valves - 2-l.5 :o rlrn o ob! F. L 4 :: (r.nq (-ilO V-ro -i l c'lA \o !O tr} ra) C) (}\o -: tr)(") r,.1 ar) (} a'; t..c? \c) f-lOooA N OC) A lo ooO A OrnOd 6(> e('f rr|trlooo.-i co a.t3<)c ai; o.\ foa Oroc.) j t;:i: s, !'-: F.o.. 5,T: rn|r]Oq \E} coc.l c.)vN Oq lt) Q tr.}\o q 61<)cn()q- ro c=a) tr}\o (> \c q 'J,::.a,: l,Vg, "5<io :dJ -, co o I ca, o -; \D@ooo oq ca6\o ooc? a.loo\DOO O a'; o\O cOooqa) \o c c.)co\coO q @\cooOq 4 c.lo\o\oO a'; c.ltr}oO -i \c@ O-; 'if(il \1'( <>-i + O -i $vc q \r0\ o $ O (^) (-- oor! OOq co Oloo q @:f o'\O<)o -i o o \lO\cN C.rOaO -; c.q r-- oO A \oa- oo A NooO-; r--m(\Ooq 1 or: rt): .t :6 |r)O OaO -t aoo O .f rrt\c|r) O r-aea (f -i +O q O \o o\ 9! O ctl Ooq O N aoq (> c) c)ooq o.F o- a.IoOOoO o\(}1 O o a'lOOOC) O O A (\ oOoe t--O O Oo r-; o .-9 o E6 -:{ q lr) V)() Oo a; \oN OA tr.)n oa A Irr tr.-O -; r,.)\o aq oor--O O-; @ ooOoQq (^) c);- Ol 90)k) Lh 6 6l o (d od(5 o' F-l br) -l ! J >\ cdo - L J anJ rl >' d) 2o ot)a =oU 0coa6 l.L- o eJ q .d (r ) a:n J ic (y'-Fl ad(.) f ? 6a <-), r) () qr() od, F q) O Fl a (J I c) r) bna p. H a :H o o:) oLc, o oo. .a (U E (t J Cdo)n\ 6 J <n (i t--.1 o 4J,JI e- t) o!(,) aifr (r1 rc C) OD H.t u (J() U) a U r. () O Hyrup Production Facility Amine Vent Emissions Source AMN VNT 0.00 3096.59 5.17 0.71 0.14 0.01 0.02 0.00 0.00 0.00 0.00 o.o2 0.00 0.00 0.58 '1.01 0.03 0.46 0.00 0.00 86.61 1258.9 119.3 152.4 22.4 18.8 27.3 25.0 170.6 1.5 39.8 5114.3 8877.1 302.7 4A32.4 2.0 0.00 TOTAL HAP 1835,1.5 TOTAL VOC 24164.5 oo o o o g d coo oo*af E€oog Ff d 0bcoo E0(t(, g ii ,o .o '6oo u. co!6)o 5 o .E u: o @! a5a- oE -9Eocb:Bo_oE6 56'E o =- @:9 Bo E, c- oo;oEo:o 6-=go -goo_--.t)o .tr E co0aJ EJ(L co'-6ao D ', .( 0ooo0 .E E(ooJ 3o a E f -_-0- -_co 6 Io (") 6 tJ) I I Y cI3 sa 0 @ oo A:.'dl D LCOD ctooEoo c3op-----)a'b co nL_/ o 9*',t417 0.426657 0.0314598 0.@431422 0.000510'ris 0.000396243 1,69679E-05 3.941?0E05 5-89217H5 l-3s168E-05 o-000306315 2.23549E-06 0,12760E-05 o-00989357 0.0145590 0.000430405 0.00573970 ,.0s516E-06 5-01754429 70_38t7 0.322309 0.0237656 0.00325t08 n,0fi234211 0-000299332 3.54808E 05 ?.a77S?E-05 t.45r'tlE-05 3 31?59E 05 0.00023't 399 1.68A75E-06 r.62396E-05 o OO7,t74'18 o.0t 09983 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E E $ g $ EEf,;FF; HE EFE E f ; ;Eg o Hyrup P roduclion Facllity Heater / Boiler Detail Sheet Source lD Number AMN HTR SCC Equiprnent lD AMN HTR Source Location Zone: Source Description Arnine Reboiler Horizontal: Equipment Usage l-leater Vertical: Equipment Make Potential operalion 8760 hr/yr Equipment Model Previous operation 0 hrSr SerialNurnber Cunenl operation 0 hr/yr Dale in Service Potential fuel usagg 92.21 MMscf/yr Equipment Configuration Previous fuel usage 0.00 MMscf&r Emission Controls None Currenl fuel usage 0.00 MMscf/yr Stack lD Staek Heighl ft Fuel Heating Value 950 Btu/scf Stack Diameter in HeatRate 10,00 MMBtu/hr ExitVelocity fVs Exit Temperature deg F Penfiit Status P.enCing Volume Flow Rate ft3/min Psten\al Emissions Pollutant Emlssion Factor Nomihal Hrs of Estimated Enrissions Source of Rating Operation Emission Faclor lb/year NOx 100 10.00 8760 .1.05 4.61 AP42 Tbl 1.4-1 co B4 10.00 8760 0.88 3:87 AF12 Tbl 1.4-1 voc 5.5 10.00 8760 0.06 0"25 AP.12 Tbt 1,4-2 SOx 0.6 10.00 8760 0.006 0.03 AP.12 Tbl 1.4-2 PM10 7 .6 10.00 8760 0.08 0.35 AP42 Tbl1.4-2 Fonnaldehyde 0.075 10.00 8760 0.00 0.00 AP42 Tbl 14-3 6.92 Benzene 0.0021 10.00 8760 0.00 0.00 AP12 Tbl 1.4-3 0.19 Toluene 0.0034 10.00 8760 0.00 0.00 AP12 Tbl 1.4-i 0.31 3.;= .F :aq€ : ;:'ts:E I Ed =38 .H >HL c, o B- -^1C.= i a eE:Ei '; 3 -8s-.(, e q r{ e H** E EE -YH L /- ',4 @eEg o r3q.Z- Z E'6Bb- o 9I it w6oYo 'tr Jo -qii O .=f>gE e >d. =Oo=5 o! ,E}.u Ee g'i_E E; EE;EE€ 8EE;58ii: 3x.6FEBEEi ici6 nr€XU EaZ I "sA E+iotr E^Z -aJ E;F€ [?gS; - ia= o* d EE E r&'Ei= sim - n € AHe - fqs?E$see.ul i tsE= 9 b iIJyOEEFEi € i#EsEg€ E EE eE AyiAEE gGS.= EIL B rli r [U'E ltv !2 " €Fr ii}: as tr 3=a eI E 5r: Y- o- '6 >\tE 6 Xsd-(Jo=oa: \-gHl-F EEH.;TgESJTYggEEET 9 doFz 'ES = =f :; FHis€EP = bH'ou q,,ii r;fE$EE;E o a, aJ- ><l- o =;ff;fE{Eg 5; I'i.;'s i fi€.sblzE,2r|= =.8 [-E p,E ; ts i(., tscJ'E-:o-d0oEF>nt(dA=;8.9 E eol9,'!-T ?a* fi *.i 9,i;q'= 2tX'=.= ,- d c0g. : ^ctEUxEqSd aU H t-.,1 X L6 a z cc t, lf ZZ:o*H AfdY'a v: FQEl 5o6xo(1 u) ;,i LJ O "-la\< ?/. &a-l hFP-r-z4ez lr- Z ao o..,) fr C-FU z u)(n z tr) : -i (.) ?- U trhrE,:Oz .- cJ flFL;.d tn rqclocq acctc oQ ca ovl- coNO\$$.ifoo€oo{-\t'ftmcov)@ Lo OL *q ov 4-o Fvgl (-) L Fru '-C€Eu.&rrl <<<8 CoOO <O pa oc)c>oooePo.+€C\<lOO&:'..:"; ;nc'r :ir- 6\ o'q.lC E9 8b a-OE"E] ar3 '. a5-5TO =Eth_o>s 5ctvz >. Fi=q'n O=qcqE ; =c.i&?osEBfE -!,-ts-:,q?Ed b" ij b9 =iAP"3g a EE gq3A9V; 3 dex Aq2 dZlY g^ 6 ,z o €s 3,TEi r = :.;; ,'r -srD=A'c66=L)-t,l-vjE--r-JJ--LL9-g 1EB 1E E -J E 3;;- - I Ut r.O o r.t = -(] -O.= ='= €,:, ='Tooaoo+ooot)lLXJ'J-oG q E E z = # a E ? ? *a3 = ? E ,=E io1 E E E EIa=E E E E#qB = E ,, 3 to:? f, f, o o aBQ 5 <5 c5 gla 5 8 ;i% 5i .5 0a AY= E Si &vZ I 7t98EMISSION COMBUSTION SOURCES1.4-5 o TABLE 1.4-2. EMISSION FACTO,RS FOR CRITERTA POLLUTANTS AND GREENHOUSE GASES FROIU NATUfuA.L GAS CO.VBUSTION" I Reference I l. Units are in pounds of pollutant per million standard cubic feet of natural gas ltred. Data are for all natural gas combustion sources. To convert frour lb/106 scf to kgii06 m3, ntultiply by 16. To convert from lb/I06 scf to lblMMBtu, divide by 1,020. The ernission factors in tlris table may be converted to other nahiral gas lreatirtg values by multiplying the given emission factor by thc ratio of the specified heatiug value to this average heating value. TOC = Total Organic Cornpounds. VOC: Volatile Or:ganic Compounds. b Based on approximately 100% conversion of fuel carbon to CO,. CO2Ub/I06 scfl = (3.67) (CON) (CXD), r';here CON : fractional conversion of fuel carbon to CO., C = carbon content of fuel by rveight (0.76), ar:d D = density of fuel, 4.2x1At lb/l06 scf. ' All PM (total, condensible, and filterable) is asstured to be less than 1.0 micrometer in diaureter. Therefore, the Pr\I emission factors presented here may be used to estimate PMro, PI\,12, or PM, emissions. Total PM is the sum of the filterable PM and condensible PN'I. Condensible Plvl is tlre particulate matter collected trsilg EPA Method 2A2 @r equivalent). Filterable PM is thc particulate matter collected on, or prior to, the filter of an EPA Method 5 (or equivalent) sampling train. d Based on 100% conversion of fuel sulfur to SOr. Assunres sulfur content is r.ratural gas of 2,000 grains/106 scf. The SOl emission factor in this table can be converted to otlrer naturai gas sulfur contents by multiplying the SO, ernission factor by tlre ratio of the site-specific sulftrr content (grains/l06 scf) lo 2,000 grains/l06 scl-. Pollutant Emission lactor (lb/i06 scf)Emission Factor Ratirtg Cort Lead NrO (Uncontrolled) NrO (Controlled-low-NO* burner) FM (Total)' PM (Condensable)" PM (Filterable)' SOru TOC Methane voc 1,20,000 0.0005 2-2 0.64 1.6 s.7 1.9 0.6 ll 2.3 5.5 A D E E D D B A B B C r.4-6 EMISS]ON FACTORS 7/98 TABLE I.4-3. E\.{ISSION FACTORS FOR SPECIATED ORGANIC COTVIPOI'NDS FROM NATURAL GT\S COM BUSTION" 91.57-6 56-49-5 83-32-9 203-96-8 720.12-7 56-55-3 7143-2 50-32-8 70s-99-2 197-24-2 205-82-3 106-97-8 218-01-9 53-70-3 25327-22-6 74-84-0 20644-A B6-73-7 50-00-0 I 1 0-54-3 193-39-5 9120-3 109-66-0 85-0 1 =8 Z-Methylnaphthaleneb'' 3 -Methylchloranthrerreu " 7, 1 2-Dimethylbenz(a)antlracenebr Acenap. hthenele Acenaphthylenebn Antlrracercb'r Benz(a)anfhraceneb;" Benzeneb Benzo(a)pyreneb" B enzo(b)fl uorantheneb' Benzo(g,h,i)peryleneb'' Benzo(k)fl uoranthenebE Butane Chryseneb" Dibenzo(a,h)anthracenebn Dichlorobe.nzeneb Ethane Fluoranthenebr Fluoreneb* Forn:aldehydeb Hexarteb Indeno(l,2,3-cd)pyreneb' ] 2.48-45 <1.8E-06 <1.68-05 <1.8E-06 <1.8E-06 <),48-06 <1.8E-06 2.18-03 <1.2E-06 <1.88-06 <1.28-06 <1.88-06 2.1E+00 <t.88-06 <1.2E-06 1.28-A3 3.1E+00 3.08-06 2.88-06 7.58-02 1.8E+00 <1.8E-06 6.lE-04 2.6E+00 l_7E-05 D E E E E E E B E E E E E E E E E E E B E E E E D 1l9B Extenral Conrbustion Sources t.4-7 o o Hyrup Production Facility Engine Detail Sheet Source lD Number Equlpment lD Source Description Engine Usage Engine Make Engine Model SerialNumber Date in Service Engine Configuration Emission Controls ISO Rating Site Rating Fuel Heating Value Heat Rate Engine Heat Rate Permit Status Potenlial Emissions 1085 hp Caterpillar 3516 TALE Horizontal: El'rG-s ENG.3 lnlet Compressor Waukesha 3516 TALE 4 slroke, lean burn 1085 BHP BHP 950 Bti/scf 8,14 MMBtu/hr 7500 Btr/hp-hr SCC Source Location Zone: Veflical: Potential operation Previous operation Current operation Potential fuel usage Previous fuel usage Current fuel usage Stack lD Stack Height Stack Diameter Exit Velocity Exit Temperature Volume Flow Rate 8760 hrlyr hr/yr hrlyr 75"04 MMscf/yr 0.00 MMscfiyr 0.00 MMsof/yr ft in ft/s 842 deg F ft3/min Polluiant Emission Factor Hrs Estimated Em Raling Operation Emission Factor ..- (lbiMMBiu)(g/hp-hr) (hp) (hrs/yr) {lb/hr) (tpy) NOx 2.00 1085 8760 4.tg 2O.gS Manufac rer CO VOC S0x PMlO Formaldehyde Acrolein Acetaldehyde 0,000588 0.0100 0.0528 0.00514 0.00836 2.00 0,50 1085 8760 4.78 20.95 Manufacturer 1085 8760 1.20 5.24 Manufacturer1085 8760 0.00 0,02 AP-42, Table 3.2-28760 0.08 0.36 AP-42, Table 3.2-2 lblyr 3763.8 366_4 595.9 1085 1 085 1085 1085 8760 8760 8760 0.43 0.04 0.07 1.BB AP-4z,fabb3.2-2 0.18 AP42, Table3.2-2 0.30 AP-42, Table 3.2-2 : o llyrup Production Facility Engine Detailsheet Source lD Number Equipment lD Source Description Engine Usage Engine Make Engine Model SerialNumber Date in Service Engine Configuration Emission Controls ISO Rating Site Rating FuelHeating Value Heal Rate Engine Heat Rate Perrnil Stalus lnlet Conrpressor Waukesha 3516 TALE 4 stroxe, lean bum 1OB5 BHP BHP 950 Btu/scf 8.14 MMBtu/hr 7500 Btuilrphr SCC Source Location Zone: Verticat: Potential operation Previous operation Current operation Potentialfuel usage Previous fuel usage Current fuel usage Stack lD Stack Height Stack Diameter Exit Velocity Exit Temperaiure Volume Flow Rate 8760 hnyr hrlyr hr/yr 75.04 MMsci/yr 0.00 MMscfiyr 0.00 MMscfiyr It in fUs 842 degF ft3/min ENG-4 ENG.4 1085 hp Caterpillar 3516 TALE Horizontal: Po{entialEmisslbns Pollutant EnrissionFaclor Hrs Estimaled Emi Source of Emission Factor 5.24 Manufacturer 0.02 AP- z,fab/e 3.2-2 0.36 AP-42, f ab]e 3.2-2 1.BB AP- z,Table3.2-2 0.18 AP-42,Table 3.2-2 0.30 AP-42,Table3.2-2 Rating Operation ..- (lb/MMBtu)(g/hp*l). (hp) . . (hrs/yr) (lb/hr) (tpy) NOx 2.00 er lblyr CO VOC SOx PMlO Formaldeh Acrolein Acetaldehy 0.000588 0.0100 0.0528 0-00s14 0.00836 0.50 1085 1085 1085 1085 1085 1085 8760 1.20 0.00 0.08 0.43 0.04 0.07 2.00 1085 8760 4.78 20.95 Manufacturer 8760 8760 8760 8760 8760 3763.8 366.4 595.9 oo o '1625 Broadway Suite 2000 Denver, CO 80202 ltla noble' \, gnefgy Tel: 303.389.3600 Fax:303.595.7410 noble energy production, inc. , subsidiary ol noble energy, inc.www. nobleenergyin c. com December 7,2005 Mr. Ram Seetharam Air Pollution Control Division Colorado Department of Public Health 4300 Cherry Creek Drive South Denver, CO 80246 SUBJECT: Additional lnformation for Noble Energy's Hyrup Production Facility Pending Air Permit Application Dear Mr. Seetharam: On November 29,I dropped off a package of additional information regarding this construction permit application and we had a brief discussion. During that discussion, you suggested that I consolidate all the fugitive emissions into a single emission point, and I also mentioned that there are some gray areas regarding the NSPS Subpart KKK applicability because of the plant's throughput. At that point, you also suggested that you would likely develop two permits: one for the "as built" equipment since the original permit had not been issued, and onl for the planned additional construction (which we are anxious to begin on or around February 1). Since that time, I have asked our engineering company for the project, Kahuna Ventures, to supply me with additional information regarding the plant. Using that information along with your suggested approach for two permits, I have prepared the attached Table l, which summarizes the emissions for the "as built" plant that exists today as well as the proposed plant expansion. Each of these cases is discussed further below. "As Built" Plant As shown in Table 1 , the "as built" emissions for the facility are 28.1tons/year (tpy) NO*, 24.6 tpy CO, 42.1tpy VOC, and 12.7 tpy total HAPs. This table incorporates the following key changes from the information submitted to you previously. l. As noted in Appendix A in an e-mail from our engineering company, the maximum throughput for the site "as built" is 8 MMscfd. Both the dehydrator contactor and existing site compression are limited to this throughput, effectively limiting the site to this throughput. The process flow diagram in Appendix A also clearly shows that the compression and dehydrator, which are "upstream" of the J-T skid, limit the throughput for the rest of the plant. oo o o e G E E U' Eo (E .9 o.e =E oo- g o(! lJ.co (, =Eo o- CL, I - -g.ct(! F -o(E(U cs9ctECo= o_ o.o_- ooaa =o)trE.oc =ooocoOcE(u Pg EH .!qtrVf,\iq,V 'S ratso-oco otr .9o .2 E u.l 6 oF ti oo ==a\al o l9o- o .e (uo a-a-(D (U O)'tr o trot eo(,Eo_.ES-{ox'a .Y .Q <.tE\tq)LE<o-o)(J EE()u o otr .9 .9, o o5 to E'tr(! co ao eoo .E rOotctft o 2. The glycol dehydrator at the site presently has a Kimray 4015 PV pump, no flash tank, and no condenser. The maximum circulation rate for this Kimray pump is 40 gallons/hr. As a result, the GLYCalc run has been re-done to reflect the lower maximum gas throughput, lower circulation rate, and absence of control equipment. The GLYCalc run has been attached in Appendix A. 3. Based on an on-site equipment count from our engineering company, we are including 275 valves and290 flanges in our fugitive counts. Most of these are in gas service; for the purposes of this estimate, we have assumed that}}Yo are in light liquid service. All of the fugitive emissions have been included in stack "JT FUG", and stack number 7 has been deleted. The revised calculations with this count are also shown in Appendix A. From a regulatory applicability perspective, NSPS Subpart KKK will apply to the whole facility because of the J-T skid. However, because the maximum gas throughput is only 8 MMscfcl, the pumps in light liquid service and valves in gas/vapor and light liquid service are exempt from the routine monitoring requirements of $60.482-2(a)(l), $60.a82-7(a), and $60.633(b)(l). This exemption is provided at $60.633(e) and effectively removes the Hyrup site from the periodic leak detection and repair program. Because the dehydrator is uncontrolled and the engines are lean burn without an oxidation catalyst, the site is a true minor "as built." Proposed Plant Expansion As we discussed on November 29, Noble is planning on installing an amine unit (including stacks AMN VNT and AMN HTR) to treat some of the higher CO2 gas that we are encountering in the area (the data associated with these two stacks was included in the November 29 submittal). Additionally, after our engineering review concluded that the plant capacity was only 8 MMscfcl, we are also currently planning a plant expansion to approximately 22 MMscfcl. This expansion will involve the following efforts: l. Additional compression The current plant only has sufficient compression for 7-8 MMscfcl. While we may be able to gain additional throughput with existing compression by selling to some lower pressure lines in the area, we are also likely going to need to add compression. We are addressing this in the permit application with the addition of units ENG-3 and ENG-4 (covered in the November 29 submittal) 2. Deltydrator modifications. To accommodate22 MMscfcl, we will need to change out the glycol pump (to a proposed Kimray 21015 PV pump with a maximum circulation of 210 gallons/lr) and add both a flash tank and a condenser. We will also have to replace the dehydrator contactor (absorber). The GLYCalc run associated with these modifications was included in the November 29 package of information. 3. Potential other modifications. Atthis poin! our engineering company is evaluating whether the J-T skid has sufficient capacity to handle 22 MMscfcl, or if additional modifications will be required for that facility. Once these modifications are completed (especially the glycol dehydrator), the facility will become a synthetic minor source for Title V because of the controls that are placed on the dehydrator to keep the facility below the25 tpy HAP threshold. Additionally, because the capacity will exceed l0 MMscfcl, then the monitoring requirements of Subpart KKK will also be applicable (i.e., the exemption will no longer apply). As a result, the fugitive emission calculations for this expansion scenario have been upAateA anO are shown in Appendix B; at this poing emissions have been estimated by assuming a z1yoin"r"*e in fugitive components, with half of the increase being in light liquid service and the other half in gas service. Control efficiencies resulting from the monitoring program were applied to these emissions. Ram, I hope this information is clear and is helpful in your work on our permit application. If you have any questions, please contact me at (303) 389-3649 or at crueter@nobleenerqyinc.com. Regards, Curtis O. Rueter, P.E. Air Quality Coordinator APPENDIX A Supporting lnformation for "As Builf'Case "ScottT. Schamp' <ScottSchamp @kahunaventur es.com> 'l2l0il2005 03:14 PM <CRueter@nobleenergyinc.com>, <jbowman@nobleenergYinc.com>To cc bcc Subject As built capacity of Hyrup Station Curtis, After reviewing the equipment that is installed at the Hyrup Station, the "as-built" capacity of the station at this time is 8 MMSCFD. The compression was designed for approximately 7 MMSCFD at site conditions, but we are modifying the suction and discharge pressure requirements to see if the units can deliver 8 MMSCFD over the near term. The dehydrator contactor and glycol pumps are also sized for a throughput of 8 MMSCFD. The JT skid on site was ordered and instalted as an 8 MMSCFD nameplate capacity. I am running process calculations on the unit at this time to determine if it can handle more volume as a part of the Hyrup expansion. Please let me know if you have any further questions. Scott T. Schamp, PE Director, Process & Project Engineering Kahuna Ventures, LLC office - (303)451-7374 fax - (303)451-7394 This message (including any attachments) contains confidential information intended for a specific individual and purpose, and is protected by law. lf you are not the intended recipient, you should delete this message. Any disclosure, copying, or distribution of this message, is strictly prohibited. o O o Hyrup Production Facility Heater / Boiler Detail Sheet Source lD Number Equipment lD Source Description JT FUG JT FUG Fugitive Emissions from J-T Skid "As Built" Count TOC Emis. Factor (lb/hr/source) % VOC 0.00992 8.24o/o 0.0055 100% 0.00529 8.24o/o 0.02866 100% 0.0194 8.24% 0.0165 100% 0.00044 8.24% 0.000463 100o/o 0.00086 8.24o/o 0.000243 100o/o 0.00441 8.24% 0.00309 100% TOTAL Equipment Valve Pump Seals Others Connectors Flanges Open-ended lines Service Gas Light Oil Gas Light Oil Gas Light Oil Gas Light Oil Gas Light Oil Gas Light Oil 220 55 0 2 't0 5 0 0 232 5B 0 0 VOC VOC (lb/hr) (tons/year) 0.180 0.788 0.303 1.325 0.000 0.0000.057 0.251 0.016 0.070 0.083 0.361 0.000 0.0000.000 0.000 0.016 0.072 0.014 0.062 0.000 0,0000.000 0.000 0.669 2.929 Page: GRI-GLYCAIC VERSION 4.0 - AGGREGATE CALCULATIONS REPORT Case Name: Hyrup Production Facility File Name= C:\t'ly Documents\Colorado\uyrup As BuiIt 120605.ddf Date: December 05, 2005 DESCRTPTION: Description: Run w/ current gas analysis and "as bui1t" (no flash Eank, no condenser, 4015 PV Kimray pump maximum flow of 40 gal/hr) Annual Hours of Operation: 8760.O hours/yr EMISSIONS REPORTS: UNCONTROLLED REGENERATOR EMISSIONS Component lbs/hr lbs/day Lons/yr Methane Ethane Propane Isobutane n-Butane Isopentane n- Pentane Cyclopentane n-Hexane Cyclohexane Other Hexanes Heptanes Metshylcyclohexane Benzene Toluene Ethylbenzene Xylenes C8+ Heavies 8.7026 t.3826 0.6951 0.l_999 0.2390 0.0987 0.0905 0.0117 0.0597 0. o960 0 -0929 0.1305 0 -]-924 0.2468 0.7501 0.0716 0 . 8151_ 0.4952 208.863 33.]-82 L6 .7 07 4.798 5.737 2.369 2 .1"72 0.280 a .434 2.305 2.230 3 - 133 4 .6L7 5 .922 1B . 003 1.71_B 19.587 11. B84 38. L175 5 .0557 3 .0490 0.8755 1, . 0469 o.4324 0.3963 0.0512 0.26L7 o.4206 0.4070 0.5718 0.8425 1.0808 3 .2855 0.3135 3.s746 2.L688 Totsa1 Total Hydrocarbon Total VOC Total IIAP Total BTEX Emissions Emissions Emissions Emissions Emissions 14.3725 1,4.3725 4.2873 L .9443 1. BB46 344 .939 344.939 102.895 46 .664 45.230 62.95L4 52.9514 t8 .17 83 8.5161 8.254s EQUIPMENT REPORTS: ABSORBER Calculated Absorber Stages: Specified Dry Gas Dew Point: TemPerature: Pressure: Dry Gas Flow Rate: 1.59 7.00 lbs. H2OIMMSCF 110.0 deg. F 900.0 psig 8. OOOO MMSCF,/day G1yco1 Losses WeE Gas Calculated Wet Gas Calculated Lean GIycoI Component wi-th Dry Gas: 0.4767 water Content: Saturated Water Content: 84.81 Recirc. Ratio: 1.54 Page: Iblhr lbs. H2OIMMSCF ga1l1b H2o Remaining Absorbed in Dry Gas i-n G1ycol Water Carbon Dioxide Nitrogen Methane Ethane Propane Isobutane n-Butane Isopentane n-Pentane Cyclopentane n-Hexane Cyclohexane Other Hexanes Heptanes Methylcyclohexane Benzene Toluene Ethylbenzene xylenes C8+ Heavies 8.24* 99.902 99.992 99 .99* 99 .98* 99.962 99.952 99.94* 99 .949-. 99.922 99.69* 99.88t 99.s02 99.91-z 99. B0? 99.48t 95.572 93.89% 92.392 B9.t2Z 99.30? 91- .7 6* 0.10t 0.018 0.01? o.022 0.04t 0.05t 0.06t 0.06t 0 .08t 0 .31? 0.L22 0.50? 0.098 o.202 o.522 4 .432 5 .11? 7.6L2 10. B8? 0.702 REGENERATOR No Stripping Gas used in regenerator. Component Rema j-ning DistilIed in Glyco1 Overhead WaLer Carbon Dioxide Nitrogen Methane Ethane Propane Isobutane n-Butane Isopentane n- Pentane Cyclopentane n-Hexane Cyclohexane Other Hexanes Heptanes Methylcyclohexane Benzene Toluene Ethylbenzene Xylenes CB+ Heavies L7 .78z 0.008 0.00? 0.00? 0.00t 0.00? 0.003 0.00? 0.242 0.27* a .41* o.32* 2 .842 0.59t 0.38t 3.57* 4 .932 7.832 10.34? t2.BBZ tL.a2Z 82.222 100.00t 100.00? 100.00t 100.00t 100.00t 100.00t 100 - 00* 99 .7 6z 99 .732 99.s92 99.682 97 .]-6* 99.412 99.622 96.43* 95.072 92.L72 89.662 87 .1-22 88 - 88t Page: STREAM REPORTS: WET GAS STREAM Temperature: 110.00 deg. F Pressure: 914.70 psia Flow Rate: 3 .34e+005 scfh Component Conc. Loadi-ng(volt) (lb/hr) Water Carbon Dioxide Nitrogen Methane Ethane Propane I sobut.ane n-Butane Isopent.ane n- Pentane Cyclopentane n-Hexane Cyclohexane Other Hexanes Hept.anes Methylcyclohexane Benzene Toluene Ethylbenzene Xylenes CB+ Heavies 1 . 79e- 001 6.72e+000 7 -79e-O02 8.41e+001 5.93e+000 l-.74e+000 3 .40e-001 3.61e-001 1 . 23e- 001 9 . 9Be- 002 4.99e-003 4.29e-002 2 -3Oe-002 7.79e-002 5 . 59e- 002 3.'l 9e-002 7.99e-003 1 - 50e- 002 9 - 98e-004 7.99e-003 4.29e-002 2.83e+001 2.60e+003 1.92e+001 1.19e+004 1.57e+003 6.74e+O02 1, .7 4e+O02 1. B5e+002 7.80e+001 5 - 34e+001 3.08e+000 3 - 26e+001 1.70e+001 5.91e+001 4.93e+001 3 .28e+001 5 .49e+000 1.21e+001 9 .33e- 001 7.46e+000 5 .44e+001 Total Components 100.00 1.75e+004 DRY GAS STREAM Temperature: 110.00 deg. F Pressure: 914.70 PsiaFlow Rate: 3.33e+005 scfh Component Conc. Loading (voI? ) (1blhr) Water Carbon Dioxide Nitrogen Methane Ethane Propane Isobutane n-Butane Isopentane n-Pentane Cyclopentane n-Hexane L.47e-OO2 6 - 73e+000 7 - 80e-002 I .43e+001 5.93e+000 1.74e+000 3.41e-001 3 . 52e- 001 1.23e-001 9.99e-Oo2 2.33e+000 2.50e+003 1 - 92e+001 1 - 19e+004 1.57e+003 6 .7 4e+O02 l -74e+OO2 1. B5e+002 7.'l 9e+00L 6 .33e+001 4.98e-003 3 .07e+000 4 .30e-002 3 .25e+001 Cyclohexane Other Hexanes Heptanes Methylcyclohexane Benzene Toluene Ethylbenzene xylenes C8+ Heavies 2.29e-OO2 7.79e-O02 5.59e-002 3.78e-002 7.55e-003 1.41e-002 9.24e-004 7 . 13e- 003 Page: l-.69e+001 5.90e+001 4.92e+001 4.27e-002 6 25e+001 25e+000 14e+001 62e-001 55e+000 39e+001 ? 5. 1. 8. 6. Total Components 100.00 1.75e+004 LBAN GLYCOL STREAM Temperature: 110.00 deg. F Ffow Rate: 6.55e-001- gpm Component Conc. Loading (wt?) (Iblhr) TEG Water Carbon Dioxide Nitrogen Methane Ethane Propane Isobutane n-Butane Isopentane n- Pentane Cyclopentane n-Hexane Cyclohexane Other Hexanes Heptanes MeLhylcyclohexane Benzene Toluene Ethylbenzene xylenes C8+ Heavies 9.84e+001 1.50e+000 6.79e-011 4.34e-014 8.24e-018 4 . 47e- 008 2.76e-0O9 6 . B5e- 010 7. B0e-010 6.38e-005 5 . 56e- 005 1 . 30e- 005 5 . 15e- 005 7.48e-OO4 1.46e-004 1.32e-004 1 - 90e- 003 3.41-e-003 1.70e-002 2.20e-OO3 3.22e-0O2 1 . 55e- 002 3.69e+002 5 .63e+000 2.55e-010 1 - 63e- 013 3 .09e-017 L.67e-0O7 1.04e-008 2.57e-009 2 .92e-OO9 2.39e-004 2 .46e-OO4 4.85e-005 1 . 93e- 004 2. B1e-003 5.48e-004 .94e-004 .12e-003 .28e-002 .31e-002 .25e-003 .21e-001 .19e-002 4 7 1 6 I 1 6 Total Components RICH GI,YCOI AND PUMP GAS STREAM 100.00 3.75e+002 Temperature: Pressure: Flow Rate: NOTE: Stream 110.00 deg. F 914 .70 psia 7.58e-001 gpm has more than one eomponent phase. Conc.(wt*) Loading ( rb/hr) TEG Water Carbon Dioxide Nitrogen Methane 79e+001 3.69e+002 55e+000 3 .16e+001 01e+0O0 4.25e+000 39e-003 1,.42e-002 08e+000 8 .70e+000 B. 7- 1-. 2 Page: Ethane Propane Isobutane n-BuLane fsopentane n- Pentane Cyclopentane n-Hexane Cyclohexane Other Hexanes Heptanes Methylcyclohexane Benzene Toluene Ethylbenzene Xylenes C8+ Heavies 3.30e-001 1.66e-001 4.7'1 e-O02 5.70e-002 2.36e-002 2.16e-OO2 2 - 80e- 003 1.43e-002 2.36e-0O2 2.23e-002 3.13e-002 4.76e-002 6.19e-002 1.94e-001 1-.90e-002 2.23e-00L 1 . 33e- 001 l-.38e+000 6.96e-001 2.00e-001 2.39e-001 9.90e-002 9.07e-OO2 1,.L7e-002 5.99e-002 9. BBe-002 9.35e-002 1.3]-e-001 1.99e-001 2.60e-001 8.14e-001 7 . 9Be- 002 9.37e-001 5.57e-001 Total Components REGENERATOR OVERHEADS STREAM 100.00 4.l-9e+002 Temperature: Pressure: Flow Rate: 2L2.OO deg. F 14 .70 psia B .29e+002 scfh Component Conc. Loading (voI&) (tblhr) Water Carbon Dioxide Nitrogen Methane Ethane Propane rsobutane n-Butane Isopent.ane n- Pentane Cyclopentane n-Hexane Cyclohexane Other Hexanes Heptanes Methylcyclohexane Benzene Toluene Ethylbenzene xylenes CB+ Heavies 5.61e+001 4.42e+00O 2.32e-002 2.48e+001 2.10e+000 7 .22e-00L 1 . 57e- 001 1 . 88e- 001 6.26e-002 5.74e-002 7.63e-003 3.L7e-002 5.22e-002 4 .93e-OO2 5.96e-OO2 8.9'7e-O02 1 .45e- 001 3.73e-001 3.09e-002 3.52e-001 1.33e-001 2.50e+001 4.25e+000 1-.42e-0O2 8.70e+000 1.38e+000 6.96e-001 2.00e-001 2 .39e-001 9.87e-002 9 . 05e- 002 1.17e-002 5.97e-002 9.60e-002 9.29e-0O2 1.31e-001 1.92e-001 2.47e-0O1, 7.50e-001 7 .L6e-0O2 I . 16e- 001 4.95e-001 ToLaI Components 100.00 4.47e+0O]- APPENDIX B Supporting lnformation for Expansion (Fugitive Calculations) oo) F-(o oo @(o oo q)60 o(E oo oo o oc, cro cro oo oi E r) {-o, o)oX 6@$ E > 9..i.jEbsg c p'il 5# 'I- t.rJ tggEI =.nEEcv:) OO rcr) OO lf)oo @o, oo \too oo oo @oo <io oo c"j ss sso1r) oo |t.- Ol'- Oro l'- l'- (Oqa? qc?oo oo (o (or@oooo $too) (o qqoo ss ss oooo ooC) ss ss ssrtro tf,o $oNO c\lo NO dr cd- (ir rJ.* OO(o@ N OO @r OO @OO rN OO l-cq qq qq oqoo oo oo o 11 <-CO r O (OX Foro o@Y=qn qq '=oo oo J FoF osEoNo>od- s ^N lf). Oo, lr)o oo)o FEE=;p*5 g .9oEoo-x tU E.= =p l<a F I-) EoLg oc .9a -o Etu(,o Qe a-.=}E trtrE, =,.c FF f'-oA -) - llo=lL(E EE I E::LC.o-YO =^'-€E 22896 oE.9L\ - 9u ^ri(DtO =.9 9.q gtrau f rf>o o croI x AWU) ss ss$o soNO NO @' @' $CO (O(f) r0)s(o €o$ soo<' oN $c.)oo oo oooo oo ooc;q oq cic;oo o) (oc\l (orr)@oe{oooc; coc{ o(')!t@ c{ oro oo c:,oo Eoooooo ? ai crE aE aE aE aEii-(uo, (Uo) oC,, oo) oo, (Uo)60= oJ o: oJ oJ o= ?6cu;io6EEqoEEF?9 F E E P 6,flSi88#oo rara GIi.) oo0(t 6,La ko I .E o 6l tD->h E.cl <o \er-o\ -oo\ I-ro\ xOo\ F-o\ Ba cno\ xao\ cao\ sr-o\ sr-o\ s {--o\ 6alr)o\ 5eF-o\ sF-o\ sr-o\ il rd F]€N \eF-o\ Bsr-o\Be acoo\ Is \e\rl t-- sra,r- \e ca ro5\r.to\ Bsc-o\ FA F-o\ sr-o\ a r={a6t\I str-o\ Nr-o\BR -o5\ coo\ @ xao\s cf) \eOco -o6\ CO xa V1o\ sr-o\ sr-o\ \atr-o\ P.( a(\l ,o6\t--o\ Bar-o\6a \atr) @ *o5\O xOo\ co Ba co Bs co *o6\la) @ xA t--o\ \ar-o\ 6aF-o\ FiO&00(\l Esr-o\ \er-o\\e io6\tr)r-sO s ca s co xo5\ co -o5\rr) F- rob\ tr-o\ sr-o\ Bsr-o\ e 00t\ \s|r)r- xAo\|r)r-6e Balr)t-\eO \a ca 6aOco xa5\ ao xSo\\o I*- \atr) F- 6alr} F- 5a|r)r- q)I f{(l) (n 6) a d td t) C) lroo. 0 cdo a J bo J d€ dJ (.) Flr a O. O. E trrJ bo J N )U' - cd 0)F al-r (.)o oU aooo cl t! r Loo. Cd U) o r€ d J bo J € dJ (d C) atroaa C)l{a U l<oO. cr3 ado (D d (H c) ()& a C)trJ o () I oA.o anco oo oU boA Oitr ((ta ar) dtra0 lr Fr L ao)& E G, Io) (ua clq) F] C, F](J F Lr q: (ho (.) q) 9 !H frl tr oO Notes: 1. Audio, visual, and olfactory walk-through inspections are applicable for inorganic/odorous and low vapor pressure compounds referenced in Section II. 2. Monitoring components in heavy liquid service is not required by any of the 28 Series LDAR programs. If monitored with an instrument, the applicant must demonstrate that the VOC being monitored has sufficient vapor pressure to allow the reduction. 3. No credit may be taken if the concentration at saturation is below the leak definition of the monitoring program (i.e. (0.044 psiall4.1 psia) x 106 = 2,993 ppmv versus leak definition = 10,000 ppmv) Valves in heavy liquid service may be given a 97Vo reduction credit if monitored at 500 ppmv by permit condition provided that the concentration at saturation is greater than 500 ppmv. Pumps in heavy liquid service may be given an 85Vo reduction credit if monitored at 2,000 ppmv by permit condition provided that the concentration at saturation is greater than 2,000 ppmv. Pumps in heavy liquid service may be given a 93Vo reduction credit if monitored at 500 ppmv by permit condition provided that the concentration at saturation is greater than 500 ppmv. If an applicant decides to monitor their connectors using an organic vapor analyzer (OVA) at the same leak definition as valves, then the applicable valve credit may be used instead of the 30Vo. If this option is chosen, the company shall continue to perform the weekly physical inspections in addition to the quarterly OVA monitoring. The 28 Series quarterly LDAR programs require open-ended lines to equipped with a cap, blind flange, plug, or a second valve. If so equipped, open-ended lines may be given a lOOTo control credit. Sample Fugitive Emission Rate Calculations Chemical Plant Implementing the 28VHP LDAR Program 4. 5. 6. 7. 8. o: .Q c.tEYo('o<o-o)o E9()o CD N{oz U, N o (uo o-a-(U o.s U) o I 9)oo.(! tr(g o fitoco1' oo o L RN \ f.\ lrt\q. B .]4 \ -\ F do o oo o o .9o't o,L o !tr C' o (l, .9 (! loo tol (e Lo tic .9oI Eo = o e tl, E Ea(/) co G' .9ao. =E oo- =o(! ILc .9 o t,o o- o-:, -; o -ct(\,F C!ocE(o Btrgo o .9o .9 E lrJ E oF oo == n\/o Hyrup Production Facility Condensate Storage Tank Emissions Detail Sheet Source lD Number Equipment lD Source Description Source Usage Location Throughput Date in Service Permit Status PotentialEmissions 6 Condensate Tank Condensate Tank Garfield County, CO 4 bbl/day 2005 Pending Source Location Zone: Horizontal: Vertical: Potential operation 8760 hr/yr Estimated Emissions Production EF (lb/bbl) (bbl/year) (tpy) VOC Benzene n-Hexane 10 0.048 0.14 1460 1460 1460 7.30 VOC 0.04 Benzene 0.10 n-Hexane 7 Hyrup Production Facility Loadout Emissions Detail Sheet Source lD Number L-1 Equipment lD SourceDescription CondensateLoadout Source Usage Condensate Loadout Source Location Zone: Horizontal: Vertical: Potentialoperation 8760 hr/yr Date in Service Permit Status Potential Emrssions Estimated Emissions (tpy) (with Potential Throughputs) 0.01 n-Hexane 0.00 Benzene 0.07 HAPs Assume 30 % Total HAPS Estimated Fugitive Emissions - Potential (See Ap42 Section 4.4) Molecular Weight of Vapors, MW 92.00 lb/lb-mol From TANKS for RVP 10 Gasoline True Vapor Pressure, Pva @ T 5.509 psia From TANKS for RVP 10 Gasoline Temperature of Bulk Liquid Loaded, T 56.01 F From TANKS for RVP '10 Gasoline 516.01 R Saturation Factor 0.6 Dedicated service Efficiency of controlled loading (%) 0.O% Annual throughput, v 61 1000 gallons Loading losses, L @ tank 7.34 lb/1000 gallons L=12.46SPMW/T(1-eff) Annualfosses @ tank, L"v 450.27 lblyr 0.23 tpy Loading Frequency 8.34286 trucks/yr Loading Duration 60 min/truck Annual Hrs of Operation 8.34 hrlyr Hourly VOC During Loading 53.97 lb/hr (while loading) (\l oE} B.o. E o) Y? * u)ooN F- r, ll" I "t{lEl; I FEI *I EEI :I 3!l sI ddt GI 60t o | =gl s lu,ul ''{ '={ ; d* ^1"al HgIBlielttolsil$ ,rrJ * "{ * E$el =trill -?il. J, I-r; I5? Ird ;{,o l" .t ol -El ? I I5l 6 El I BI : El E =l o Snanil? Nnr,oml'o' n, on r -^'. xoGE(ls 'ooo €o.baOEx=g6 6-ol{: .96'E>3 aixqEF(! OFILO*b)'=(u!{ !.oEE+?3U)*.6 X [E fl#EgE;oo.9A- EI, IJJ J