Technical and Economic Evaluation of Supercritical...

Technical and Economic Evaluation of Supercritical Oxy-combustion for

Utility Scale Power Generation Dr. Aaron McClung

Sr. Research Engineer, Southwest Research Institute, San Antonio, TX USA [email protected]

Dr. Klaus Brun

Program Director, Southwest Research Institute, San Antonio, TX, USA [email protected]

Dr. Lalit Chordia

President, Thar Energy L.L.C., Pittsburgh, PA USA [email protected]

mailto:[email protected]



Outline

• Project Participants • Fossil based sCO2 systems

– Typical characteristics • Coal fired oxy-combustion

– Cycle layouts – Predicted performance – Component Technology Readiness Levels

• Direct fired natural gas oxy-combustion – Cycle concepts – Anticipated challenges

Southwest Research Institute • Independent, nonprofit applied research and

development organization founded in 1947 • Eleven technical divisions

– Aerospace Electronics, Systems Engineering & Training

– Applied Physics – Applied Power – Automation & Data Systems – Chemistry & Chemical Engineering – Engine, Emissions & Vehicle Research – Fuels & Lubricants Research – Geosciences & Engineering – Mechanical Engineering – Signal Exploitation & Geolocation – Space Science & Engineering

• Total 2013 revenue of $592 million – 38% Industry, 36% Govt., 26% Govt. Sub – $6.7 million was reinvested for internal

research and development • Over 2,800 staff

– 275 PhD’s / 499 Master's / 762 Bachelor's

• Over 1,200 acres facility in San Antonio, Texas

– 200+ buildings, 2.2 million sq. ft of laboratories & offices

– Pressurized Closed Flow Loops – Subsea and High Altitude Test Chambers – Race Oval and Crash Test Track – Explosives and Ballistics Ranges – Radar and Antenna Ranges – Fire testing buildings – Turbomachinery labs

Benefiting government, industry and the public through innovative science and technology

2.1 Miles

1.2

Mile

s

SwRI Machinery Program • Fluids & Machinery Engineering Department

– Mechanical Engineering Division (18) • Capabilities

– Root cause failure analysis – Rotordynamic design/audit – Pipeline/plant simulation – CFD and FEA analysis – Test rig design – Performance testing

• Recent Commercial Projects – Test stands for LNG and CNG process evaluation – Air Cycle Machine Design, Build, and Test – Numerical Propulsion System Simulation® (NPSS®)

Consortium Management • Recent DOE sCO2 Programs

– Physical Properties • High-Pressure Gas Property Measurements

– CO2 Pipeline and Compression • CO2 Pipeline Pulsation Analysis and Mitigation • Novel Concepts for the Compression of Large Volumes of CO2 (FC26-05NT42650)

– sCO2 Turbomachinery • Development of a High Efficiency Hot Gas Turbo-Expander and Low Cost Heat Exchangers for Optimized CSP Supercritical CO2

Operation (DE-EE0005805) • Electrothermal Energy Storage with A Multiphase Transcritical CO2 cycle (DE-AR0000467) • Physics-Based Reliability Models for Supercritical CO2 Turbomachinery Components (DE-FOA-0000861, PREDICTS) • Utility-Scale sCO2 Turbomachinery and Seal Test Rig Development (DE-FOA-0001107) Oxy-combustion • Novel Supercritical Carbon Dioxide Power Cycle Utilizing Pressurized Oxy-combustion In Conjunction With Cryogenic Compression

(DE-FE0009395) • High Inlet Temperature Combustor for Direct Fired Supercritical Oxy-Combustion (DE-FE0024041)

– Heat Exchangers • High Temperature, High Pressure Compact Heat Exchanger Development (DE-FOA-0001095) • Development of a Thin Film Primary Surface Heat Exchanger for Advanced Power Cycles (DE-FOA-0001095)

Thar companies: Thar Energy LLC Systems for fuel production, power generation

and geothermal heating and cooling Thar Process, Inc. Supercritical fluid process design and toll

extractions from organic feedstocks

Shown here: Pharmaceutical production system … Good Manufacturing Process … Supercritical fluid extraction

Core competencies: 25+ years commercializing “Green”

supercritical fluid technologies (SCF)

Designer and developer of supercritical fluid processes, systems & major components

Industrial scale 24/7/365 installations, world wide:

Food Chemicals Nutraceutical Pharmaceutical Chemical

Heat exchangers for high pressure, high temperature application

FOSSIL BASED SCO2 SYSTEMS

“Typical” sCO2 Cycle Conditions Application Organization Motivation Size [MWe] Temperature [C] Pressure [bar]

Nuclear DOE-NE Efficiency, Size 300 - 1000 400 - 800 350

Fossil Fuel DOE-FE Efficiency, Water Reduction

500 - 1000 550 - 1200 150 - 350

Concentrated Solar Power

DOE-EE Efficiency, Size, Water Reduction

10, 100 500 - 1000 350

Shipboard Propulsion

DOE-NNSA Size, Efficiency 10, 100 400 - 800 350

Shipboard House Power

ONR Size, Efficiency < 1, 1, 10 230 - 650 150 - 350

Waste Heat Recovery

DOE-EE ONR

Size, Efficiency, Simple Cycles

1, 10, 100 < 230; 230-650 15 - 350

Geothermal DOE-EERE Efficiency, Working fluid

1, 10, 50 100 - 300 150

Cycle Efficiency

0.4

0.45

0.5

0.55

0.6

0.65

0.7

600 700 800 900 1000 1100 1200 1300

Ther

mal

Effi

cien

cy

Temperature (C)

Recompression Cycle at 290 bar

Recompression (290 bar)

DESIGN -SPECDSPLIT

CALCU LATORPOST

TRANSFE RT-PRES

B1

SPLIT1

MIXER1

HXLOW

Q=159430

HXHIGH

Q=992454

PRECOOL

Q=-123554

COOL

Q=-0

COMP2

W=33235

COMP1

W=24847

EXPANDER

W=-279879

DUMMY

Q=345891

CALCULATORT-DUMMY

1220.00

293.84

1.00000

0.01027

1.00

S1

-279879S10

33235S16

24847

S17

-221798

WPOWERW

80.11

83.96

1.00000

0.00598

1.00S480.11

83.96

0.65000

0.00388

1.00

S1180.11

83.96

0.35000

0.00209

1.00S5

204.65

293.84

0.35000

0.00102

1.00S7

203.66

293.84

0.65000

0.00189

1.00

S14

204.00

293.84

1.00000

0.00291

1.00

S8

206.66

85.26

1.00000

0.01017

1.00

S3

73.07

293.84

0.65000

0.00094

1.00

S13

1017.80

86.86

1.00000

0.02874

1.00S2

958.57

293.84

1.00000

0.00858

1.00

S9

30.00

82.96

0.65000

0.00111

0.00S12

204.65

293.84

0.35000

0.00102

1.00S6

1220.00

293.84

1.00000

0.01027

1.00

PHOT1

Temperature (C)

Pressure (bar)

Mass Flow Rate (kg/sec)

Volume Flow Rate (cum/sec)

Vapor Fraction

Q Duty (Wat t)

W Power(Wat t)

Fossil Based sCO2 Power Cycles • Competiton

– Indirect: Supercritical Steam with CCS – Direct: Natural Gas Combined Cycle

• Advantages – High power efficiencies at “Moderate” temperatures – Oxy-combustion facilitates integrated carbon capture – Compact turbomachinery lead to compact power blocks

• Offset by recuperation to achieve high cycle efficiencies • Challenges

– 250 C thermal input temperature widow is not ideal for combustion based systems

• 400 C Combustor inlet for 650 C Turbine Inlet • 950 C Combustor inlet for 1200 C Turbine inlet

– Flue gas cleanup for direct fired systems – Efficiency losses for indirect cycles

High Temperature Recompression Cycle

DESIGN -SPECDSPLIT

CALCU LATORPOST

TRANSFE RT-PRES

B1

SPLIT1

MIXER1

HXLOW

Q=159430

HXHIGH

Q=992454

PRECOOL

Q=-123554

COOL

Q=-0

COMP2

W=33235

COMP1

W=24847

EXPANDER

W=-279879

DUMMY

Q=345891

CALCULATORT-DUMMY

1220.00

293.84

1.00000

0.01027

1.00

S1

-279879S10

33235S16

24847

S17

-221798

WPOWERW

80.11

83.96

1.00000

0.00598

1.00S480.11

83.96

0.65000

0.00388

1.00

S1180.11

83.96

0.35000

0.00209

1.00S5

204.65

293.84

0.35000

0.00102

1.00S7

203.66

293.84

0.65000

0.00189

1.00

S14

204.00

293.84

1.00000

0.00291

1.00

S8

206.66

85.26

1.00000

0.01017

1.00

S3

73.07

293.84

0.65000

0.00094

1.00

S13

1017.80

86.86

1.00000

0.02874

1.00S2

958.57

293.84

1.00000

0.00858

1.00

S9

30.00

82.96

0.65000

0.00111

0.00S12

204.65

293.84

0.35000

0.00102

1.00S6

1220.00

293.84

1.00000

0.01027

1.00

PHOT1

Temperature (C)

Pressure (bar)



Vapor Fraction

Q Duty (Wat t)

W Power(Wat t)

968 C 1220 C

30 C

221 kWe

345 kWth

1 kg/s

ηth = 64%

COAL FIRED OXY-COMBUSTION

Development of a Supercritical Oxy-combustion Power Cycle with 99% Carbon Capture

Southwest Research Institute® and Thar Energy L.L.C. • Engineering development, technology

assessment, and economic analysis used to evaluate technical risk and cost of a novel supercritical oxy-combustion power cycle

• Optimized cycle couples a coal-fired supercritical oxy-combustor with a supercritical CO2 power cycle to achieve 40% efficiency at low firing temperature, 650 C

– Cycle is limited by TRL of critical components

• COE $121/MWe with 99% carbon capture – 49% increase over Supercritical Steam

Without Carbon Capture ($81/MWe), exceeding the 35% target

– 21% reduction in cost as compared to Supercritical Steam with 90% Carbon Capture ($137/MWe).

• Phase 1 completed in September 2013 • Budget $1.25 million • Ready to demonstrate supercritical oxy-

combustor and critical low TRL technologies

Project Scope • Evaluate a novel supercritical oxy-combustion power cycle

for meeting the DOE goals of: – Over 90% CO2 removal for less than 35% increase in cost of

electricity (COE) when compared to a Supercritical Pulverized Coal Plant without CO2 capture

• Cycle evaluation based on: – Cycle and economic modeling to qualify cost and cycle

performance – Technology gap assessment to identify critical low TRL

components and technologies – Bench scale testing to back up cycle models and evaluate state

of low TRL technologies • Propose development path to address low TRL components

Proposed Cycle: Cryogenic Pressurized Oxy-combustion (CPOC)

• Transcritical cycle (gas, liquid, and supercritical states)

• Leverage iso-thermal compression to minimize compression work

DE-FE0009395 Project Closeout 2/21/2014

Proposed Cycle: Supercritical Oxy-combustion

• Leverages recent SunShot and DOE-NE cycles development

• Efficiencies up to 60% possible for the power block


Indirect CPOC Layout

CO2 +H2O (SC steam)

Sequestration Ready CO2

Fossil Fuel, Ch4+

Pure Oxygen

Water Separation / Flue gas clean-up

Turbo Expander

Power output, to Electrical

Generator

Power Input

Oxy-Combustion

Chamber

CO2 Cryo- Pump

Refrigeration Heat

Exchanger

Power Input

Isothermal Co2

compressor

CO2 at atm. Conditions: 15 psia, 98°F

H2O + residuals

CO2 + H2O (liquid)

5000 psia, 982°F

5000 psia, 20°F

Supercritical CO2

2200 psia, 20 °F

300 psia, 0°F

Liquid CO2

300psia, 100°F

CO2 gas

sCO2 to sCO2 Heat

Exchanger Cyclone

Separation

Supercritical CO2

sCO2 Pump 2200 psia,

20°F

2200 psia, 20°F

Fly Ash + Particulates

2200 psia, 1000°F

2200 psia, 20°F

Power Input

Coal Fired Indirect Supercritical Oxy-combustion Cycle Configuration

HXMAIN1 HXCLEANPRECOOL

HXLOW HXHIGH

EXPANDER

COMP1

COMP2

P6 P7a

P8

P1

P2

P3

P5

P7b

P7

P4

P4b

Combustor

O2

Coal Slurry

C2

C3

C4

FLUE GAS CLEANUP

C5C6

C0

Sequestration Ready CO2

High Temperature Power LoopRecompression sCO2 Power Cycle

Combustion LoopCoal Fired Supercritical Oxy-Combustion

H2O, CaCO2, CaSO4, Hg

H2O, O2, CaCO2

COOLING OUT

COOLING INBOOST

BOOST C7

P4a

CYCLONE

C1

C1b

Power Block Thermal Loop Overall

Efficiency [%] 48 Thermal 78.9 HHV / 81.8 LVH 37.9 HHV / 39.3 LHV

CO2 Flow [kg/s] 4887 4930 Recycle

P high / P low [atm] 290 / 82 100 / 93

T high / T low [C] 650 / 20 653 / 78

Indirect Cycle Model with Supercritical Oxy-Combustor

MIX-COAL

CYCLONERGIBBS

Q=-182132974

SLRYPUM P

CALCULAT ORC-YIELD

RYIELD

Q=182132974

MIX1

HEAT-AUX

Q=0

CALCULAT ORASU WM IX1

HXMAIN1

Q=1230727570

SPLIT

Q=0

DE SIGN-SPECC-COAL

DE SIGN-SPECCO2M ASS

CALCULAT ORC-RECY

HXCLEAN

Q=2275090230

BOOSTW=18889203

S-SEQ

B6

Q=0

CALCULAT ORC-PRES

HIERARCHY

PWR1

DE SIGN-SPECP1MDOT

CALCULAT ORPOST-CYC

NET-SUM

CALCULAT ORTHPWR1

DE SIGN-SPECCO2TEMP

B4

W=3607442

CALCULAT ORC-SLRY

B1

Q=0

DE SIGN-SPECH20-BAL

DE SIGN-SPECT-H20

30.00

1.0000

70.6260COAL-IN

30.00

1.0000

0.0000H2O-IN

29.92

1.0000

70.6260SLRYLOWP

653.00

99.0000

5107.6395

PRODUCTS

653.00

97.0000

5101.7970

CHOT

653.00

97.0000

5.8425SOLIDS

30.00

100.0000

107.2103

O2-IN

453.77

100.0000

4929.8033

CO2-RET

100.0000

70.6260SLRYHIGP

450.00

100.0000

70.6260S10

0.0000

RY-BYPAS

29.84

100.0000

70.6260RY-IN

450.00

100.0000

70.6260

IN-BURN

-182132974.00

QBURN

29.84

100.0000

70.6260SLRY-HOT

48030200.10

WASUW

48030200.10

CWNET

0.00

WSLRPMP

456.77

96.0000

5101.7970

CMID

453.77

290.0000

4887.0782PCOLD1

650.00

290.0000

4887.0782PHOT1

453.77

100.0000

4929.8033

CO2-RET1

78.33

93.0000

5062.0485CL-CO2

78.33

93.0000

132.2452

TOSEQ

78.33

93.0000

4929.8033

CLEAN3

78.71

94.0000

6135.3682

CLEAN1

78.33

93.0000

1073.3198

CL-H2O

100.47

95.0000

5101.7970WCOLD

84.88

100.0000

4929.8033

CLEAN2

-604112926.00

WPOWER1

-533556589.00

WNETW

18889203.10

WCLEAN

650.00

290.0000

4887.0782

PHOT1B

121.80

149.7000

132.2452

PIPELINE

3607442.02

SEQ-COM P

30.00

95.0000

1033.5712

H2O-SCRU

Temperature (C)

Pressure (atm)


Duty (Watt)

Power(Watt)

Q Duty (Watt)

W Power(Watt)

Cleanup

DE SIGN-SPECH20-FRAC

DE SIGN-SPECH2O-SFRA


EXPANDER

W=-846993775

COMP1

W=103709586

COMP2

W=139171263

COOL

Q=-0

PRECOOL

Q=-626685163

HXHIGH

Q=1902612830

HXLOW

Q=781401058

MIXER1

SPLIT1

CALCULAT ORPOST

TRANSFE RT-PRES

B1

DE SIGN-SPECDSPLIT

DUMMY

Q=0

650.00

290.0000

4887.0782

S1

509.27

85.7242

4887.0782S2

177.72

84.1451

4887.0782

S3

59.98

82.8621

4887.0782S4

59.98

82.8621

1710.4774S5

174.72

290.0000

1710.4774S6

174.72

290.0000

1710.4774S7

174.72

290.0000

4887.0782

S8

453.77

290.0000

4887.0782

S9 PCOLD1(OUT)

20.00

81.8752

3176.6008S12

49.92

290.0000

3176.6008

S13

174.72

290.0000

3176.6008

S14

650.00

290.0000

4887.0782

S15PHOT1(IN)

-846993775.00S10139171263.00S16

59.98

82.8621

3176.6008

S11

103709586.00

S17

-604112926.00

WPOWER WPOWER1(OUT)

Temperature (C)

Pressure (atm)


Power(Wat t)

Q Duty (Wat t)

W Power(Wat t)

Power Block Cleanup

Combustor

Combustion Loop TRL Component/Sub-system Technology Type

Operating Conditions

Assumed or Specified Performance Characteristics

Assumptions Regarding Anticipated Application Issues

Technology Readiness

Inlet Outlet

Tem

pera

ture

[C

]

Pres

sure

[atm

]

Tem

pera

ture

[C

]

Pres

sure

[atm

]

Combustion Loop Coal Pulverizer Generic 25 1 25 1 < 9 kw-h/ton TRL 9 Slury Pump Generic 25 1 30 92.25 60% Efficiency TRL 9 Supercritical oxy-combustor New vertical flow swirl

combustor 450 95 93 92.25 98+% combustion efficiency Combustor to be

demonstrated in Phase 2 TRL 6 at the

completion of Phase 2 demonstration

Dry pulverized coal feed Supercritical CO2 slurry 25 1 <450 110 Minimal added water content TRL 2 Dry pulverized coal feed Posimetric Pump 25 1 <450 110 Dry feed Demonstrated systems can

not achieve pressure ratio TRL 4

Removal of solid products of combustion

Lock-hopper 703 92 80 1 Fluid and thermal losses, impact on efficiency unknown

TRL 4

Cyclone Separator Generic 703 93 703 91 98% Removal 3 atm dP

Materials considerations and thermal insulation for hot gas

cleanup

TRL 9

Recouperator (HXMAIN) Compact micro-channel heat exchanger

703 91 460 88 5 C Pinch Point 3 atm dP

See Note 3 TRL 7, See Note 1

Pre-heater (HXCLEAN) Compact micro-channel heat exchanger



Sulfur Cleanup Under evaluation for hot, high pressure cleanup

162 85 ? ? Under Evaluation to identify technologies compatible with loop conditions

High efficiency requirements drive the need for hot, high

pressure cleanup

TRL 5 - 9 depending on

cleanup conditions Water Removal Under evaluation for hot, high

pressure cleanup 162 85 ? ? Under Evaluation to identify technologies

compatible with loop conditions High efficiency requirements drive the need for hot, high

pressure cleanup

TRL 5 - 9 depending on

cleanup conditions Boost Pump Generic 150 80 95 Seals and materials for

supercirtical CO2 TRL 9

Air Separation Unit Cryogenic 30 1 450 93 140 kWh/t for 95% O2 based on literature TRL 9

Note 1: TRL 7 at the completion of a compantion DOE SunShot Project in 2016 (DE-EE0005804)

Note 2: TRL 7 at the completion of a compantion DOE SunShot Project in 2013 (FC26-05NT42650)

Note 3: Materials and manufacturing assumptions for cost and performance

Note 4: Turbomachinery layout and design is being adressed in other DOE sponsored programs (DE-EE0005804)

Power Loop TRL

Component/Sub-system Technology Type

Operating Conditions

Assumed or Specified Performance Characteristics

Assumptions Regarding Anticipated Application Issues

Technology Readiness

Inlet Outlet

Tem

pera

ture

[C

]

Pres

sure

[atm

]

Tem

pera

ture

[C

]

Pres

sure

[atm

]

Power Loop Supercritical CO2 Recompression Cycle

TRL 7, See Note 1

sCO2 Turbo-expander 650 290 509 86 90+% efficiency See Note 4 TRL 7, See Note 1

Recouperator (HXHIGH) Compact micro-channel heat exchanger



Recouperator (HXLOW) Compact micro-channel heat exchanger



sCO2 Pump/Compressor 70 83 190 290 05+% efficiency See Note 4 TRL 7, See Note 2

sCO2 Pump/Compressor 25 82 60 290 05+% efficiency See Note 4 TRL 7, See Note 2

Pre-cooler Compact micro-channel heat exchanger



Note 1: TRL 7 at the completion of a compantion DOE SunShot Project in 2016 (DE-EE0005804) Note 2: TRL 7 at the completion of a compantion DOE SunShot Project in 2013 (FC26-05NT42650) Note 3: Materials and manufacturing assumptions for cost and performance Note 4: Turbomachinery layout and design is being adressed in other DOE sponsored programs (DE-EE0005804)

Development Path • 1 MWth Supercritical Oxy-combustor

Demonstration • Test bed for technology development

– Supercritical oxy-combustor – Particulate cleaning of the compact

microchannel heat exchanger – Solids injection at pressure – Solids removal at pressure

• Advance technologies from TRL 2, Technology Concept, to TRL 6, Pilot Scale System Demonstrated in a Relevant Environment

• Operate with coal water slurry, plan for dry feed or sCO2 slurry extension

Supercritical Oxy-combustor Cyclone

Separator

Underflow Particulate Separation

Boost Compressor Water

Scrubber

Supercritical Oxy-combustor

Cyclone Separator

Underflow Particulate Separation

Water Scrubber

Cooling Tower

SwRI Oxy-Combustor Concept • Pulverized coal + water slurry

– Recycle water from combustion loop cleanup

– Water provides flame temperature control

• Rotating impeller fuel injector – Optimize shear-mixing of slurry,

CO2, and O2 – Controlled fuel injection rate

through impeller, O2 injection controls flame position

• CO2 cooled liner – Flame position, diffusion, and

dilution control – Flame centering – Wall temperature buffering

Coal Slurry

Liner Casing

Impeller

sCO2 O2

Mixing Zone

Motor

O2

Startup: Fuel (NG, Oil) + Pilot/Torch Igniter


Combustor Design • Designed to feed a coal-water

slurry and O2 into supercritical CO2 – Inlet Temperature 450 C (842 F) – Inlet Pressure 96.5 bar (1400 psi) – Firing Temperature 700 C (1292 F)

• Limited data on coal combustion at elevated pressures

• Combustor design through simulation, augmented with coal combustion properties testing

• Flow rates at 550 MWe – Coal 50 kg/s – O2 80 kg/s – H2O 50 kg/s – CO2 4000+ kg/s

Rotary Atomizer

O2 Feed

Coal-water slurry feed

CO2 Feed

Combustion zone

CO2 Feed

Inner liner

Concept

Analysis

Design

Oxy-Combustion Test Loop • Major components

– Charge Compressor or Pressurized CO2 Feed – Combustor

• Oxygen feed • Coal slurry feed

– Cyclone separator • Solids removal and handling

– Recuperater – Water scrubber and cleanup

• Liquid removal and handling • CO2 removal and handling

– Cooling Tower – Boost Compressor

• Operating Conditions – 450 – 650 C (800 – 1200 F) – 102 atm (1500 psi)

• Flow Rates: 1 MWth – 3.4 kg/s Hot side flow rate – 3.2 kg/s CO2 recycle – 0.05 kg/s Coal feed – 0.08 kg/s O2 Feed – 4.25 kg/s H2O Recycle

HXCLEAN

Combustor

O2

Coal SlurryC2

C4

FLUE GAS CLEANUP

C5C6

C0

Coal Fired Supercritical Oxy-Combustion Test Loop

H2O, Products of Combustion

H2O

BOOST

C7

CYCLONE

C1

C1b

CO2 Capture and Disposal

Underflow Particulate Removal

CO2H2O

Solids

DIRECT NATURAL GAS FIRED OXY-COMBUSTION

High Inlet Temperature Combustor for Direct Fired Supercritical Oxy-Combustion

Southwest Research Institute® and Thar Energy L.L.C.

• Cycle analysis and optimization for large scale, direct fired supercritical oxy-combustion for power generation – Based on engineering development and technology assessment – Target 52% plant efficiency to compete with NGCC – Requires 64% cycle efficiency – Turbine inlet 1220 C at 290 bar

• Evaluate technology readiness level of critical cycle components – Key known low TRL component: supercritical Oxy-combustor – Initial design of a high pressure, high temperature natural gas

fired oxy-combustor • Phase 1 award negotiations in progress

Initial Cycle: Cryogenic Pressurized Oxy-combustion (CPOC)

• Transcritical cycle (gas, liquid, and supercritical states)

• Leverage iso-thermal compression to minimize compression work

Recuperated CPOC

High temperature recuperator • Hot stream: Turbine outlet • Cold stream: Low temperature recuperator • Assume 10 C pinch point Low temperature recuperator • Hot stream: Iso-thermal compressor outlet • Cold stream: Dense phase pump • Assume 5 C pinch point

Performance tweaks • Iso-thermal compressor

– Reduce pressure ratio (Increases refrigeration requirements)

– Assume 20% of adiabatic temperature rise • Turbine inlet pressure between 145 and 175 bar • Assume 5C of sub-cooling for refrigeration

COMBUST

Q=1300359EXPANDER

W=-963172

REFHX

Q=-385489

CRYOPUMP

W=51900

B6

COMP

W=81204

RECOUPH

Q=451878

DESIGN-SPECD-TINOUT

CALCULATORC-CL-T

CALCULATORC-CRYOP

RECOUPL

Q=10103

183.57

175.00

1.00000

0

1.00

S1

1200.00

175.00

1.00000

0

1.00

S2 435.57

1.00

1.00000

1

1.00

S3

-19.22

5.00

1.00000

0

1.00S4

-62.27

5.00

1.00000

0

0.00

S5

-36.34

175.00

1.00000

0

0.00

S6

-963172

S8

81204

S9

51900S10

-830067

WNETW

-20.83

1.00

1.00000

0

1.00

S12

183.57

175.00

1.00000

0

1.00

S13

-30.83

175.00

1.00000

0

0.00

S14

-31.34

5.00

1.00000

0

1.00

S7

Temperature (C)

Pressure (bar)

Mas s Flow Rate (kg/s ec)

Volume Flow Rate (cum/s ec)

Vapor Frac tion

Q Duty (Watt)

W Power(Watt)

ηth = 63.8%

Add high temperature recuperator after expander, low temperature recuperator after compressor

183 C

1220 C

-62 C

830 kWe

1300 kWth

1 kg/s

High Temperature Recompression Cycle

DESIGN -SPECDSPLIT

CALCU LATORPOST

TRANSFE RT-PRES

B1

SPLIT1

MIXER1

HXLOW

Q=159430

HXHIGH

Q=992454

PRECOOL

Q=-123554

COOL

Q=-0

COMP2

W=33235

COMP1

W=24847

EXPANDER

W=-279879

DUMMY

Q=345891

CALCULATORT-DUMMY

1220.00

293.84

1.00000

0.01027

1.00

S1

-279879S10

33235S16

24847

S17

-221798

WPOWERW

80.11

83.96

1.00000

0.00598

1.00S480.11

83.96

0.65000

0.00388

1.00

S1180.11

83.96

0.35000

0.00209

1.00S5

204.65

293.84

0.35000

0.00102

1.00S7

203.66

293.84

0.65000

0.00189

1.00

S14

204.00

293.84

1.00000

0.00291

1.00

S8

206.66

85.26

1.00000

0.01017

1.00

S3

73.07

293.84

0.65000

0.00094

1.00

S13

1017.80

86.86

1.00000

0.02874

1.00S2

958.57

293.84

1.00000

0.00858

1.00

S9

30.00

82.96

0.65000

0.00111

0.00S12

204.65

293.84

0.35000

0.00102

1.00S6

1220.00

293.84

1.00000

0.01027

1.00

PHOT1

Temperature (C)

Pressure (bar)



Vapor Fraction

Q Duty (Wat t)

W Power(Wat t)

968 C 1220 C

30 C

221 kWe

345 kWth

1 kg/s

ηth = 64.1%

Efficiency Comparison

0.2

0.25

0.3

0.35

0.4

0.45

0.5

0.55

0.6

0.65

0.7

600 800 1000 1200 1400

Ther

mal

Effi

cien

cy

Temperature (C)

Recompression (290 bar)

Recuperated CPOC(150/5 bar)Recuperated CPOC(150/10 bar)Baseline CPOC (300/20bar)

CPOC Recompression Efficiency 63.85% 64.00% Turbine Inlet Temp (C) 1200 1200 Turbine Inlet Pressure (bar) 150 290 Turbine Outlet Pressure (bar) 1 100 Mass flow (kg/s) 1.00 1.00 W net (MW) 0.830 0.221 Q in (MW) 1.300 0.345 HX high (MW) 0.451 0.992 HX low (MW) 0.010 0.154

Total Recuperation (MW) 0.461 1.146

Scaled to 550 MWe plant, parasitic losses neglected CPOC Recompression

Mass flow (kg/s) 662.65 2,488.69 W net (MW) 550.00 550.00 Q in (MW) 861.45 858.60 HX high (MW) 298.86 2,468.78 HX low (MW) 6.63 383.26 Total Recuperation (MW) 305.48 2,852.04

Recuperated CPOC performs on par with the recompression cycle, has larger thermal input window, higher power density, and requires less recuperation

QUESTIONS

APPENDIX

Initial CPOC Power Block Analysis

CPOC w/out Combustion

PUMP

EXPANDER

HEATIN

HEATOUTB10B1

DE SIGN-SPECB2

B3

CALCULAT ORB4

DE SIGN-SPECB5

5000

56162

0.00

0

5000

56162

1.00

1

14

56162

1.002

300

56162

0.00

4

-59098

1585

9

394

10

-3930

WNETW

7795216

6Q

5000

56162

0.00

5

300

56162

1.00

3

7081080

S3

7081080

QCOOLQ

Thermal Efficiency

sCO2 Recompression Power Block

sCO2 w/out Combustion

EXPANDER

COMP1

COMP2

RECEIVER

COOL

PRECOOL

HXHIGHHXLOW

MIXER1

SPLIT1

CALCU LATORPOST

TRAN SFERT-TEMP

TRAN SFERT-PRES

S1

S2

S3

S4

S5S6

S7

S8

S9

S11

S12

S13 S14

S15

Thermal Efficiency

Efficiency Comparison

Technical and Economic Evaluation of Supercritical...

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