DELTA PURIFICATION’S SOLVENT RECLAIMER … · • Electro-dialysis; capable of removing HSS only ... Delta Reclaimer™ Process Diagram; September 8, 2015 PCCC3, Regina, SK, Canada,

September 8, 2015 PCCC3, Regina, SK, Canada, September 8 - 11, 2015 1

DELTA PURIFICATION’S SOLVENT RECLAIMER OPERATION AND PERFORMANCE IN THE CLEAN-UP OF DEGRADED SOLVENTS USED IN CO2 CAPTURE FROM COAL-FIRED POWER PLANT FLUE GASES

Dr. Ahmed Aboudheir, P.Eng.President, Delta Purification, Regina, SK, CanadaD W lid ElM di P EDr. Walid ElMoudir, P.Eng.Senior Process Engineer, HTC CO2 Systems, Regina, SK, Canada

Delta Technology forSeptember 8, 2015 PCCC3, Regina, SK, Canada, September 8 - 11, 2015 2

Delta Technology for Cleanup Degraded Solvents and Glycols

R l i


ReclaimerR l i it i d i d t f th l t• Reclaimer unit is designed to remove from the solvent:• high-boiling degradation products, • ionic species (heat stable salts, HSS),ionic species (heat stable salts, HSS), • impurities and fine suspended solids.

• The type of degradation products is a function of:• the impurities in the gaseous streams, • the solvent type, • the operating conditions of the acid gas absorption plantthe operating conditions of the acid gas absorption plant.

• The type of reclaiming processes• Ion Exchange; capable of removing HSS only• Electro-dialysis; capable of removing HSS only• Thermal distillation, capable of removing of HSS, degradation

products, and solidsproducts, and solids

T f Th l R l i i U


Types of Thermal Reclaimers in UseK ttl l i f i i MEA d DGA• Kettle reclaimer for primary amines; MEA and DGA solvents. Operated at the stripper pressure in order to return the reclaimer product vapour to the stripper. Main p p ppdisadvantages:• Extensive Energy use

L l f t hi h i l d l t• Large volume of waste, which include solvent • Reclaimer unit operated under reduced pressure for

secondary and tertiary amines; DEA, DIPA and MDEA.secondary and tertiary amines; DEA, DIPA and MDEA. Main disadvantage:• Amines reclaimed on a contract basis on-site using mobile units or

off site at high costoff-site at high cost• Use of complex design units (High CAPEX & OPEX)• Require highly experienced operators

Potential Problems from Accumulation ofSeptember 8, 2015 PCCC3, Regina, SK, Canada, September 8 - 11, 2015 5

Potential Problems from Accumulation of Degradation Products in Solvents

R d ti i l t b ti it• Reduction in solvent absorption capacity• Change of solvent physical properties leads to change

the solvent characteristics and performancethe solvent characteristics and performance.• Foaming and increased solvent foaming tendency in

absorber/stripper reduce the contact area between gas pp gand liquid phases.

• Increasing solvent corrosivity due to accumulation of corrosive species such as Heat Stable Saltscorrosive species, such as Heat Stable Salts.

• Degradation products and heat stable salts lead to increase the replacement/change-out of mechanical andincrease the replacement/change out of mechanical and activated carbon filters and solvents makeup, which will increase the operating and maintenance costs.

Delta Reclaimer™ Advantages Compared to


Delta Reclaimer Advantages Compared to Existing Technologies• Less capital cost• Less operating cost• Less waste for disposal• Less utility consumptionsLess utility consumptions• Simple to operate and maintaina ta

• Higher recovery rate for solvent

• Reclaims single, mixed, and formulated solvents

D lt R l i I t ti t th SVM CO C t Pl t


Delta Reclaimer Integration at the SVM CO2 Capture Plant

Delta Reclaimer™ Process Diagram;September 8, 2015 PCCC3, Regina, SK, Canada, September 8 - 11, 2015 8

Delta Reclaimer Process Diagram;Patented Technology


Delta Reclaimer Main Operating Parameters

• Saturated low pressure steam at 40 psig R l i ti t• Reclaimer operating at an absolute pressure of 190 mmHg (Torr)mmHg (Torr)

• Reclaimer operating temperature 180 to 205°Ftemperature 180 to 205 F

• Cooling water at 75 °F• Chemical injectionChemical injection

• 28 wt% Soda ash or • 50 wt% Caustic soda


Samples of the Main Process Streams

• Colours of the Samples from right to left; Reclaimer Feed, Reclaimer Product, and Process FluidProduct, and Process Fluid

Collected concentrated Waste for• Collected concentrated Waste for Disposal on a Continues Basis


Solvent recovery rate and energy consumption

Process Data Run No. 1 Run No. 2 Run No. 3Reclaimer Operating Pressure, 190 190 190Reclaimer Operating Pressure, mmHg 190 190 190

Reclaimer Operating Temperature °F 185 ±5 185 ±5 200 ±5Temperature, FChemical Injection for neutralization

28 wt% Na2CO3

28 wt% Na2CO3

50 wt% NaOH

Average total impurities, wt% 1.45 5.80 8.50

Total Solvent Recovery % 98% 95% 91%Total Solvent Recovery, % 98% 95% 91%

lb saturated steam (40 psig)per lb product 0.97 1.1 0.95per lb product

R # 1 S l l i


Run # 1: Sample analysisProcess Streams Feed Product

MEA Concentration, wt% 17.51 17CO2 loading, mol/mol 0.085 0.128

Specific gravity 1.0393 1.013R f ti I d t 20 oC 1 3636 1 352Refractive Index at 20 oC 1.3636 1.352

pH with CO2 10.4 10.65pH without CO2 10.91 11.39

Heat stable salts (HSS), wt% as MEA 1.24 0.15( )

OrganicHSS

T. Formate, ppm 846 13T. Acetate, ppm 793 9

T. Glycolate, ppm 289 78T Oxalate ppm 372 78T. Oxalate, ppm 372 78

Inorganic HSSSulfate, ppm 8,656 25

Chloride, ppm 6,452 16Nitrite, ppm 68 0

N (hydroxyethyl) glycine ppm 3 874 0Degradation

Products

N-(hydroxyethyl)-glycine, ppm 3,874 0N-(N-hydroxyethyl-ethylamine)-

ethylenediamine, ppm 15 0

Heavy metals Fe ppm 5 0 3Heavy metals Fe, ppm 5 0.3

R # 2 S l l i



MEA C t ti t% 16 75 17 04MEA Concentration, wt% 16.75 17.04CO2 loading, mol/mol 0.100 0.120

Specific gravity 1.0485 1.0145

Refractive Index at 20 oC 1 3673 1 3493Refractive Index at 20 C 1.3673 1.3493pH with CO2 10.42 10.57

pH without CO2 10.91 11.25Heat stable salts (HSS), wt% as MEA 1.18 0.23

OrganicHSS


T. Glycolate, ppm 424 11T. Oxalate, ppm 356 185pp



N-(hydroxyethyl)-glycine ppm 4 771 16Degradation

Products


ethylenediamine, ppm 7 ‐

Heavy metals Fe, ppm 7 0.1y , pp

R # 3 S l l i



MEA C t ti t% 17 25 16 87MEA Concentration, wt% 17.25 16.87CO2 loading, mol/mol 0.070 0.055

Specific gravity 1.0705 1.023

Refractive Index at 20 oC 1 3701 1 3492Refractive Index at 20 C 1.3701 1.3492pH with CO2 10.51 10.94

pH without CO2 ‐ 11.17Heat stable salts (HSS), wt% as MEA 1.105 0.1

OrganicHSS


T. Glycolate, ppm 477 141T. Oxalate, ppm 284 94pp



N-(hydroxyethyl)-glycine ppm 4 291 0Degradation

Products


ethylenediamine, ppm ‐ ‐

Heavy metals Fe, ppm 4.8 0.1y , pp


Heat stable salts of feed and product streamsFeed (Run 1) Product (Run 1)

1.50,( ) ( )

Feed (Run 2) Product (Run 2)Feed (Run 3) Product (Run 3)

1.00

1.25

e Sa

ltsM

EA

0.50

0.75

Stab

le%

as

M

0 00

0.25

Hea

t S wt

0.000 2 4 6 8 10 12 14 16 18 20 22 24

Data Point

R 2 I iti t ti i i t


Run 2: Impurities concentration in main streams1,000,000 Feed Product Waste

10 000

100,000

or H

eat

n pmFeed Product Waste

1,000

10,000

Prod

uct o

alt A

nion

atio

n , p

p

10

100

datio

n P

Stab

le S

aon

cent

ra

1

Deg

rad S

Co

MEA Trimer = N-(N-hydroxyethyl-ethylamine)-ethylenediamineHEGly = N-(hydroxyethyl)-glycineHEGly N (hydroxyethyl) glycine

C l i & Fi di


Conclusion & Findings• Excessive contaminated solvent has been restore to almost its

original purity: colorless, 17 wt% MEA & minimum impurities.• Low Operating Cost;

• 98% recovery rate for solvents with 1.5 wt% contaminants &98% recovery rate for solvents with 1.5 wt% contaminants &• 91% recovery rate for solvents with 8.5 wt% contaminants • Energy consumption 1 lb steam (40 psig) per 1 lb product• Easy to operate and maintainEasy to operate and maintain• Minimum attention from the plant operator.

• Minimum waste for disposal, concentrated waste was collected periodically while the reclaimer process was in continuous operationperiodically while the reclaimer process was in continuous operation.

• Low Capital Cost; simple process configuration and few unit operations Reclaims single mixed and formulated solvents• Reclaims single, mixed, and formulated solvents

• Assist the CO2 Capture Plants to meet the production capacity and cleanup targets at minimum operating cost, emission to atmosphere,

d t f di land waste for disposal

A k l d


Acknowledgment• The support provided by the SVM staff, engineers and technicians to operate the Delta Reclaimer at SVM facility,

• The detailed lab analysis of the feed, product, yand waste samples by:• Dr. Gary Rochelle, University of Texas, AustinDr. Gary Rochelle, University of Texas, Austin• Mr. Paul Nielsen, University of Texas, Austin

THANK YOUSeptember 8, 2015 PCCC3, Regina, SK, Canada, September 8 - 11, 2015 19

THANK YOU …

F i f tiFor more information:Ahmed Aboudheir002 – 2305 Victoria AveR i SK S4P 0S7 C dRegina, SK, S4P 0S7, [email protected]+1-306-352-6132+1-306-501-8227+1 306 501 8227

Documents

DELTA PURIFICATION’S SOLVENT RECLAIMER … · • Electro-dialysis; capable of removing HSS only ... Delta Reclaimer™ Process Diagram; September 8, 2015 PCCC3, Regina, SK, Canada,