high performance and low cost reclaiming … presentation 2019.pdf · purification for the energy...

PURIFICATION FOR THE ENERGY AND BIOMASS INDUSTRIES

HIGH PERFORMANCE AND LOW COST RECLAIMING TECHNOLOGY FOR SOLVENT, ETHANOL & GLYCOL RECLAIMING, RECYCLING, AND REUSING

Delta Reclaimer Technology 1


Delta Technology for Cleanup Degraded Solvents and Glycols



Reclaimer• Reclaimer unit is designed to remove from the solvents:

• high-boiling degradation products, • 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 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 solids



Types of Thermal Reclaimers in Use• 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 disadvantages:• Extensive energy use• Operating cycle is very short• Could lead to solvent thermal degradation • Neutralization of HSS usually is incomplete • Large volume of waste generated which includes solvent

• Reclaimer unit operated under reduced pressure for secondary and tertiary amines; DEA, DIPA and MDEA. Main disadvantages: • Amines reclaimed on a contract basis on-site using mobile units or off-site at high

cost• Use of complex design units (High CAPEX & OPEX)• Require highly experienced operators • Could lead to solvent thermal degradation • Neutralization of HSS could be incomplete • Purging some of fluids (solvent) inside the vessels are quite frequent to maintain

stable operation.



Potential Problems from Accumulation of Degradation Products in Solvents• Reduction in solvent concentration and its absorption capacity• Change of solvent physical properties leads to change the solvent characteristics

and performance which would affect the operation of unit operations such as absorption towers, pumps and heat exchangers.

• Foaming and increased solvent foaming tendency in absorber/stripper reduce the contact area between gas and liquid phases.

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

• Increase the potential of equipment fouling and plugging. • Cause an increase of emissions• Cause an increase in the energy consumption for solvent regeneration• Degradation products and heat stable salts lead to increase 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 Existing Technologies

• Simple System Design • Less capital cost• Less operating cost• Less waste for disposal• Less utility consumptions• Simple to operate and maintain• Higher recovery rate for solvent• Reclaims single, mixed, and formulated amine solvents or glycols



Delta Reclaimer Integration at the SVM CO2 Capture Plant



Delta Reclaimer™ Process Diagram;Patented Technology in USA, Canada, Europe, China, Australia

October 16, 2018 Delta Reclaimer Technology 8


Control Room &Reclaimer Control Screen


Remote Access to the Reclaimer Operation


Delta Reclaimer Main Operating Parameters at SVM

• Saturated low pressure steam at 40 psig

• Reclaimer operating at an absolute pressure of 190 mmHg (Torr)

• Reclaimer operating temperature 180 to 205°F

• Cooling water at 75 °F• Chemical 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 Fluid

• 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, mmHg 190 190 190

Reclaimer Operating Temperature, °F 185 ±5 185 ±5 200 ±5

Chemical 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%

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



Run # 1: Sample analysisProcess Streams Feed Product

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

Specific gravity 1.0393 1.013Refractive 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 78

Inorganic HSSSulfate, ppm 8,656 25

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

Degradation Products

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

ethylenediamine, ppm 15 0

Heavy metals Fe, ppm 5 0.3




MEA 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 1.3493pH with CO2 10.42 10.57

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

OrganicHSS







ethylenediamine, ppm 7 -

Heavy metals Fe, ppm 7 0.1




MEA 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 1.3492pH with CO2 10.51 10.94

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

OrganicHSS







ethylenediamine, ppm - -

Heavy metals Fe, ppm 4.8 0.1



Heat stable salts of feed and product streams


0.00

0.25

0.50

0.75

1.00

1.25

1.50

0 2 4 6 8 10 12 14 16 18 20 22 24

Hea

t Sta

ble

Salts

,w

t% a

s M

EA

Data Point

Feed (Run 1) Product (Run 1)Feed (Run 2) Product (Run 2)Feed (Run 3) Product (Run 3)


Run 2: Impurities concentration in main streams


1

10

100

1,000

10,000

100,000

1,000,000

Deg

rada

tion

Prod

uct o

r Hea

t St

able

Sal

t Ani

on

Con

cent

ratio

n , p

pm

Feed Product Waste

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


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 &• 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 maintain• Minimum attention from the plant operator.

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

• Low Capital Cost; simple process configuration and few unit operations

• 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, and waste for disposal



THANK YOU …


www.deltapurification.com

Marketing: Jeff Allison – (306) 530-6025 #149 333 Riverfront Ave. SE Calgary, Alberta Canada T2G 5R1

http://www.deltapurification.com/

high performance and low cost reclaiming … presentation 2019.pdf · purification for the energy...

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