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![Page 1: Amine Thermal Degradation By: Jason Davis. Overview Carbamate Polymerization of MEA Background Chemistry Model PZ and MEA/PZ Blends Amine Screening.](https://reader036.fdocuments.in/reader036/viewer/2022062308/56649eb65503460f94bbfbc7/html5/thumbnails/1.jpg)
Amine Thermal Degradation
By: Jason Davis
![Page 2: Amine Thermal Degradation By: Jason Davis. Overview Carbamate Polymerization of MEA Background Chemistry Model PZ and MEA/PZ Blends Amine Screening.](https://reader036.fdocuments.in/reader036/viewer/2022062308/56649eb65503460f94bbfbc7/html5/thumbnails/2.jpg)
Overview
Carbamate Polymerization of MEABackgroundChemistryModel
PZ and MEA/PZ Blends
Amine Screening
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Amine Losses
Oxidative Degradation – A. Sexton Thermal Degradation – degradation
occuring at stripper and reclaimer conditionsCarbamate polymerizationOther thermal degradation
Volatility – M. Hilliard Physical Losses
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STRIPPERABSORBER CROSSX
FLUEGAS
EFFLUENT
COLDRICH
HOTRICH
HOTLEAN
COLDLEAN
CO2
RECLAIM
Amine Losses
Vapor Losses Oxidative Degradation
Thermal Degradation
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Thermal Degradation
Industry standards currently limit MEA concentration at 30wt% (15wt% being the standard for natural gas treating) due to concern over increased corrosion and thermal degradation
Degradation can lead to ineffective CO2 capture, loss of expensive solvent, increased equipment corrosion, and an increased environmental impact
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Chemistry
NH2OH
NHOH CO2-
NHOH CO2-+ CO+ CO22
NHO
O
2-Oxazolidone2-Oxazolidone
+ H+ H22OO
MEA CarbamateMEA CarbamateMEAMEA
+ H+ H++
+ H+ H++
Polderman Dillon and Steele (1955)
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Chemistry - Continued
NNH
O
OH
NNH
O
OH + H+ H22OO
1-(2-hydroxyethyl)-2-imidazolidone1-(2-hydroxyethyl)-2-imidazolidone
(HEIA)(HEIA)
+ H+ H22OO NH
OH NH2 + CO+ CO22
N-(2-hydroxyethyl)-ethylenediamineN-(2-hydroxyethyl)-ethylenediamine
(HEEDA)(HEEDA)
NHO
O
+ + MEAMEA
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What Do We Know
MEA Carbamate Polymerization Factors CO2 loading Temperature Amine concentration
Literature for MEA No kinetic data available Controlled when solutions held at 15 wt% in
industrial applications
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Sample Apparatus
Use high pressure sample containers made of 316L stainless steel tubing and endcaps
Forced convection oven to maintain constant temperature for a large number of samples
Maintains CO2 loading in solution at elevated temperature and pressure to accelerate thermal degradation
Simple experimental design and allows for a large number of solutions to be tested at one time
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Analytical
GC High temperatures can alter results Separation of polar compounds difficult and cross
contamination in sample port HPLC
Amine detection difficult with standard detectors Can identify and quantify nonionic species
Cation IC Separates positively charged ions Will not detect non-ionic species Can measure amine disappearance and the
formation of ionic species (highly polar)
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MEA Experiments
Matrix of samplesMEA Concentration (15-40wt%)CO2 Loading (0.2-0.5)Temperature (100-150oC)
100oC and 150oC experiments in 2ml sample containers
120oC and 135oC experiments in 10ml containers
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11m MEA after 8 wks at 135oC
0.0 1.3 2.5 3.8 5.0 6.3 7.5 8.8 10.0 11.3 12.5 13.8 15.0 16.3 17.5 18.8 20.0-0.50
2.00
4.00
6.00 10172007 135C 11m Autosampler #6 [modif ied by TEXAS UNIVERSITY OF] 11m MEA a=0.5 T=135C t=8wks ECD_1µS
min
1 - MEA - 3.525
2 - Unknown 1 - 5.7503 - HEEDA - 12.150
MEA
HEEDA
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Emperical Data Regression
tMEAKof
oeMEAMEA *** 5.045.1
)987.1*/(289004.33 TeK where K is the temperature dependent rate constant given by:
MEAf = final MEA concentration (molality)
MEAo = initial MEA concentration (molality)
= Loading defined as moles CO2 per mole amine
t = time (weeks)
T = Temperature (K)
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Effect of Loading (T=135C)
4
5
6
7
8
9
10
11
0 2 4 6 8
Time (wks)
ME
A (
mo
lali
ty) =0.2
=0.4
=0.5
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0
1
2
3
4
5
6
7
0 2 4 6 8
Time (wks)
ME
A (
mo
lalit
y)
Effect of Temperature (=0.4)
150oC
135oC
120oC
100oC
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Effect of Concentration (T=135oC =0.4)
50
55
60
65
70
75
80
85
90
95
100
0 1 2 3 4 5 6 7 8
Time (wks)
ME
A R
emai
nin
g (
%)
11m
7m 3.5m
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HEEDA Formation 11m MEA at 135oC
0
0.05
0.1
0.15
0.2
0.25
0.3
0.35
0.4
0.45
0.5
0 2 4 6 8
Time (weeks)
HE
ED
A
(m)
=0.2
=0.4
=0.5
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Thermal Degradation Costs
Approximately $2/ton CO2 allocated to solvent make-up in most cost models Assumes 1.5kg MEA/ton CO2 and a cost of $1.32/kg
MEA 3.5m MEA, P=1atm, $0.10/ton CO2
11m MEA, P=2.5 atm, ~$1.60/ton CO2
Does not include corrosion or reclaimer costs Natural gas processing experience says reclaimer
composes 50% of thermal degradation Corrosion has been shown to increase in the
presence of HEEDA
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MEA Conclusions
Temperature has the greatest effect on thermal degradation in the stripper Quadruples every 15oC Double pressure = 15oC temp increase
Loading increases degradation slightly more than 1st order
Concentration has multiple effects Slightly more than 1st order in concentration In practice an increase in concentration yields increased
stripper temperatures due to increased BP of solution (3.5m to 11m increases temperature by ~4oC and increases thermal degradation by 40%)
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MEA/PZ Blended Systems
Made measurements of aqueous PZ and a 7m MEA/2m PZ blend at varying temperatures
PZ not expected to degrade since it does not have an alcohol group to form an oxazolidone intermediate
Unknown what the blended system would do
NH NH
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Aqueous PZ after 8 weeks at 150oC
0.0 1.3 2.5 3.8 5.0 6.3 7.5 8.8 10.0 11.3 12.5 13.8 15.0 16.3 17.5 18.8 20.0-0.50
1.25
2.50
3.75
5.00 7m MEA 2m PZ Tests #11 [modif ied by TEXAS UNIVERSITY OF] 2.5m PZ T=150 t>8wks ECD_1µS
min
1 - Piperazine - 13.100PZ
These peaks are in the time 0 sample
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Degraded MEA/PZ after 3 weeks at 135oC
0.0 1.3 2.5 3.8 5.0 6.3 7.5 8.8 10.0 11.3 12.5 13.8 15.0 16.3 17.5 18.8 20.0-1.0
5.0
12.0
1 - 7m MEA 2m PZ Tests #7 [modif ied by TEXAS UNIVERSITY OF] 7m MEA 2m PZ t=0 ECD_12 - 7m MEA 2m PZ Tests #4 [modif ied by TEXAS UNIVERSITY OF, 1 peak manually assigned] ECD_1µS
min
21
1 - MEA - 3.525
2 - Piperazine - 12.975
MEA
PZ
Degradation Products
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Amine Losses after 2 Weeks
Solvent Temp (oC)
MEA Loss (%)
PZ Loss (%)
Total Amine
Loss (%)
Pure PZ 120 - <2.0 <2.0
Pure MEA 120 4.0 - 4.0
MEA/PZ Blend
120 5.0 8.6 6.3
Pure PZ 135 - <2.0 <2.0
Pure MEA 135 18.1 - 18.1
MEA/PZ Blend
135 11.9 31.8 19.1
*All systems have a loading of 0.4 and similar moles of alkilinity
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PZ Blend Conclusions
PZ with a loading of 0.4 did not degrade at 150oC for over 8 weeks
The blended systems preferentially destroyed PZ, the more expensive solvent
PZ is a stronger nucleophile so it attacks the MEA oxazolidone structure more readily than MEA thereby increasing degradation
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Other Amines
Set up several screening experiments on other amine systems including EDA DETA MDEA HEEDA DGA AMP
Only measured ionic degradation products
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Amine Screening(T=135oC =0.4 t=4wks)
Amine Concentration (molality)
Remaining Amine Peak (%)
Total Area Retention (%)
PZ 3.5 100 100
DGA 7 93 98
MDEA 50 wt% 71 97
AMP 3 97 96
EDA 3.5 64 91
MEA 7 76 80
DETA 2.3 9 71
HEEDA 3.5 3 17
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MDEA after 4wks at 135oC
1.0 2.0 3.0 4.0 5.0 6.0 7.0 8.0 9.0 10.0 11.0 12.0 13.0 14.0 15.0 16.0 17.0 18.0 19.0 20.0-0.50
1.00
2.00
3.00
4.00
1 - 135 Amine Screening Autosampler #11 [modif ied by TEXAS UNIVERSITY OF] 50wt% MDEA a=0.45 t=0 (2) ECD_12 - 135 Amine Screening Autosampler #12 [modif ied by TEXAS UNIVERSITY OF, normalized] ECD_1µS
min
21
1 - 4.350MDEA
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HEEDA after 4wks at 135oC
0.0 1.3 2.5 3.8 5.0 6.3 7.5 8.8 10.0 11.3 12.5 13.8 15.0 16.3 17.5 18.8 20.0-0.50
1.25
2.50
3.75
5.50
1 - 135 Amine Screening Autosampler #3 [modif ied by TEXAS UNIVERSITY OF] 3.5m HEEDA a=0.45 t=0 ECD_12 - 135 Amine Screening Autosampler #4 [modif ied by TEXAS UNIVERSITY OF] 3.5m HEEDA a=0.45 T=135 t=4wks ECD_1µS
min
21
1 - HEEDA - 11.942HEEDA
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Amine Screening Conclusions
HEEDA degrades very quickly compared to other amines studied
Industrially MDEA does not significantly degrade but this study shows it does shift to other amines Arm shifting Higher activation energy than other amines so
increased temperature might effect more
Order from least to most degradation PZ<DGA< MDEA< AMP<EDA< MEA< DETA<
HEEDA
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Future Work
Mechanistic model for MEA degradation MEA with spikes of various degradation products
to determine k values for reactions Measure HEIA formation with HPLC for low temp
samples to get a more accurate degradation rate
Thermal Degradation modeling in ASPEN Various stripper configurations Possible reclaiming simulations as well
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Summary Thermal degradation can be important in the overall
cost of the MEA absorber/stripper system Engineering controls can keep these costs reasonable Further study of the reclaiming system is needed
PZ does not thermally degrade by itself, but does in the presence of alkanolamines
Many common amines do degrade under stripper conditions and this should be considered when choosing a solvent
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QUESTIONS?