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
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(L
T
Eo
LNo
c
F-
Jo-c
o-I
E(,
L(o
I
fo
o_I
E(,
L(!
o)
c
9
_c
o
-c.
_o
:J
co
-c
D
o
Eo
Yo(o
o
tr
O l-
aococ
a
C)Eo
C
o
0)a
o'If
o
=
L
0)
3o
o_o
Cal
!o
0)o-
U)
x
L-,c)
F
O
JE
OI
z
O
LLa
co
3o
LL
3oq
EX
tU
o
Eq)tcx
IU
E
.goix
TU
-c.
.9)
0.)r
.vooa
=oo
o,
.c,x[J
Bo
u_
q,
l
t1^
(o
(oooE
.9
U'
.9
E
JJ
I
s'a
Lo
(I]o
Scan31 9, November 04, 2005.max
v@Ir)
N
Nf)Nt)
o\r
o
nL/
Page:GRI-GLYCalc VERSION 4.O - AGGREGATE CALCULATIONS REPORT
Case Name: Hyrup Production FaciLityFil-e Name: D:\Rinko LLC\E1y Env\Air permit\Emissions inventory\g1y run22 . ddf
Date: March 17 , 2OO5
DESCRI PTION:
Description:
Annual Hours
Noble Energy, Inc.
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
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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
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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
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nlL'
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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
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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
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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
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2.5049
N-DECANE
N-UNDECANE
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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
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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
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o-000306315
2.23549E-06
0,12760E-05
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0.0145590
0.000430405
0.00573970
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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
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7t98EMISSION COMBUSTION SOURCES1.4-5
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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
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1l9B Extenral Conrbustion Sources t.4-7
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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
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'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.
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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)
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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
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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)
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