ADVANCED COGENERATION SYSTEMS - - ADVANCED COGENERATION SYSTEMS A - - PowerPoint PPT Presentation

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ADVANCED COGENERATION SYSTEMS - - ADVANCED COGENERATION SYSTEMS A - - PowerPoint PPT Presentation

Sep 02, 2023 216 likes •553 views

Institut Teknologi Teknologi Bandung Bandung, Indonesia , Indonesia Institut Fakultas Teknologi Teknologi Industri Industri - - Departemen Departemen Teknik Teknik Kimia Kimia Fakultas 30 March March 2010 in 2010 in Bandung Bandung

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SLIDE 1

Institut Institut Teknologi Teknologi Bandung Bandung, Indonesia , Indonesia Fakultas Fakultas Teknologi Teknologi Industri Industri -

  • Departemen

Departemen Teknik Teknik Kimia Kimia 30 30 March March 2010 in 2010 in Bandung Bandung

ADVANCED COGENERATION SYSTEMS ADVANCED COGENERATION SYSTEMS -

  • A DESALINATION

A DESALINATION-

  • POWER PLANT

POWER PLANT-

  • CONCEPT

CONCEPT Dr. Dr.-

  • Ing. Claudia Werner
  • Ing. Claudia Werner

Technische Universit Technische Universitä ät Berlin, Germany t Berlin, Germany

Fachgebiet Anlagen- und Sicherheitstechnik Fachgebiet Anlagen- und Sicherheitstechnik

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SLIDE 2

Dr.-Ing. Claudia Werner

CONTENT

  • 1. Introduction
  • 2. State of the Art of Desalination/Electricity Production
  • 3. Combination - Desalination Plant/CCGT Plant
  • 4. Recent Research - Thermoeconomics and Optimisation Approaches
  • 5. Simulation Process
  • 6. Results of the Simulation Process
  • 7. Conclusion and Outlook
  • 8. Acknowledgement
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SLIDE 3

Cogeneration is the simultaneous production of heat and power in a single thermodynamic process Cogeneration systems such as CCGT power plants or block heat and power plants are available on the market Application is motivated by different issues of climate protection Advanced cogeneration systems:

  • Combined production of

Electricity/District Cooling

  • Combined production of

Electricity/Chemicals

  • Combined production of

Electricity/Fresh Water

Dr.-Ing. Claudia Werner

  • 1. INTRODUCTION - Cogeneration Systems

Source: http://www.vattenfall.de, 2010.

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SLIDE 4
  • 1. INTRODUCTION - Water Supply/Water Withdrawal

Dr.-Ing. Claudia Werner

Increasing world water withdrawals since 1900

Source: http://www.worldwatercouncil.org, 2010.

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SLIDE 5

Dr.-Ing. Claudia Werner

  • 1. INTRODUCTION - Withdrawal to Availability Ratio

Source: Konishi,T. Global Water Issues and Nuclear Seawater Desalination, 2010.

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SLIDE 6

18,000 island, 6,000 inhabited by 215 million people endowed with 5,590 rivers flowing over 5,500 km³/year

  • f water

annual amount of precipitation in the range of 1,000 mm to 5,000 mm fresh water supply by shallow water wells and deep water ground surface annual water resources in Indonesia: 1,690 x 10³ m³/km² or 16.8 x 10³ m³/capita intrusions of seawater detected in Jakarta, Medan, Semarang, Surabaya

and Ujung Pandang

Dr.-Ing. Claudia Werner

  • 1. INTRODUCTION - Situation in Indonesia

Source: www.weltkarte.com, 2010 .

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SLIDE 7

Dr.-Ing. Claudia Werner

  • 1. INTRODUCTION - Water Resource and Water Demand

358,813 156,850 3,221,000 Indonesia 1,886 589 981,000 Mollucas+Papua 23,093 8,204 1,008,000 Borneo 49,583 25,298 738,000 Sumatra 77,305 25,555 247,000 Celebes 42,274 13,827 60,000 Lesser Sunda 164,672 83,378 187,000 Java 2015 2000 (mill. m³/year) (mill. m³/year) Water Demand Water Resource Island(s)

Source: Sunaryo, G. R. Prospect on Desalination and other non-electric Applications of Nuclear Energy in Indonesia, 2010.

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SLIDE 8

Thermal Processes

  • Multi Effect Distillation (MED)
  • Multi Stage Flash (MSF)
  • Thermal Vapor Compression (TVC)

Non-Thermal Processes

  • Reverse Osmosis (RO)
  • Mechanical Vapor Compression (MVC)

Desalination Projects in Indonesia

  • Fossil Desalination Projects (Pulau Seribu, Sulawesi)
  • Nuclear Desalination Projects (Madura Island)
  • Renewable Desalination Projects (Cituis)

Thermal Processes

  • Multi Effect Distillation (MED)
  • Multi Stage Flash (MSF)
  • Thermal Vapor Compression (TVC)

Non-Thermal Processes

  • Reverse Osmosis (RO)
  • Mechanical Vapor Compression (MVC)

Desalination Projects in Indonesia

  • Fossil Desalination Projects (Pulau Seribu, Sulawesi)
  • Nuclear Desalination Projects (Madura Island)
  • Renewable Desalination Projects (Cituis)
  • 1. INTRODUCTION - Desalination Processes and Projects

Dr.-Ing. Claudia Werner

Source: Konishi,T. Global Water Issues and Nuclear Seawater Desalination, 2010.

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SLIDE 9
  • 2. STATE OF THE ART - Desalination Plants

Dr.-Ing. Claudia Werner

Multi Effect Distillation (MED)

Typical capacity: 500 - 18,000 m³/d Electric consumption: 1 - 2.5 kWh/m³ Heat consumption: 150 - 260 MJ/m³ Product salinity: < 10 ppm TDS Facility: Telde & Las Palmas - Gran Canaria Multi Effect Distillation Process

Source: http://www.ide-tech.com, 2009.

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SLIDE 10
  • 2. STATE OF THE ART - Desalination Plants

Dr.-Ing. Claudia Werner

feed product sole final condenser

stage 1 steam stage 2 stage 3 condensate

steam from CCGT steam to CCGT

sole

feed product sole final condenser

stage 1 steam stage 2 stage 3 condensate

steam from CCGT steam to CCGT p1 > p2 > p3 T1 > T2 > T3

  • H. Müller-Holst: Mehrfacheffekt-Feucht-

luftdestillation bei Umgebungsdruck, 2002.

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SLIDE 11
  • 2. STATE OF THE ART - Desalination Plants

Dr.-Ing. Claudia Werner

Reverse Osmosis (RO)

Typical capacity: 1 - 10,900 m³/d Electric consumption: 4 - 9 kWh/m³ Product salinity: < 500 ppm TDS

product concentrate feed HP PUMP pretreat- ment posttreat- ment

  • H. Müller-Holst: Mehrfacheffekt-Feuchtluftdestillation bei Umgebungsdruck, 2002.
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SLIDE 12
  • 2. STATE OF THE ART - Hybrid Desalination Plants

Dr.-Ing. Claudia Werner

Increased flexibility in desalination plant management Economic aspects of hybrid desalination plants Modulation of the Power-to-Water-Ratio (PWR) as required

MED MED-

  • MSF

MSF MED MED-

  • MSF

MSF-

  • VC

VC MED MED-

  • VC

VC MED MED-

  • RO

RO

Thermal Thermal ratio ratio of hybrid MED

  • f hybrid MED plants

plants Figure: Hybrid desalination plants based on MED according to the thermal ratio

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SLIDE 13
  • 2. STATE OF THE ART - Hybrid Desalination Plants

Dr.-Ing. Claudia Werner

MED/RO in parallel connection

  • independent operation of the

desalination units (MED/RO)

  • complete sharing of the energy

supply, the water pre- and post- treatment as well as the product and sole removal facilities

  • examples (parallel connection):

Jubail (Saudi Arabia) Madina-Yanbu (Saudi Arabia)

common intake MED plant RO plant

  • utfall

product

Source: M. A. Helal, et al.: Optimal design of hybrid RO/MSF desalination plant, 2003.

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SLIDE 14
  • 2. STATE OF THE ART - Hybrid Desalination Plants

electric power requirement (MED/RO) 1.3 kWh/m³ / 6.5 kWh/m³ (3) steam recirculation (MED) 66 t/h / 1.1 bar / 102 °C (2) steam requirement (MED) 66 t/h / 1.1 bar / 157 °C (1)

Dr.-Ing. Claudia Werner

product water feed (seawater) Hybrid desalination plant MED Plant

A2

RO Plant

A1 A3

sole

Total Total desalination desalination capacity capacity = 2 x 17,500 m = 2 x 17,500 m³ ³/d /d MED MED capacity capacity / RO / RO capacity capacity = 1 = 1 : : 1 1

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SLIDE 15
  • 2. STATE OF THE ART - Electricity Production (750 MW)

Dr.-Ing. Claudia Werner

CCGT Seabank Power Station - Electric base and mid-load supply

Source: Kraftwerksschule Essen e.V.

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SLIDE 16

low pressure parameter 36.2 t/h / 4.8 bar / 235 °C medium pressure parameter 52.1 t/h / 30 bar / 320 °C reheat parameter 247.6 t/h / 28.5 bar / 550 °C high pressure parameter 253.3 t/h / 110 bar / 550 °C

Electricity Production: CCGT Seabank Power Station

Triple-pressure process and single reheat CCGT Power Station on natural gas basis Electricity yield: 57.8 %

Dr.-Ing. Claudia Werner

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SLIDE 17
  • 3. COMBINATION - Desalination plant/CCGT plant

Dr.-Ing. Claudia Werner

flue gas product water feed (seawater) CCGT power plant air natural gas gas turbines HRSG steam turbines Hybrid desalination plant MED Plant

A2

RO Plant

A1 A3

sole electric power

electric power requirement (MED/RO) 1.3 kWh/m³ / 6.5 kWh/m³ (3) steam recirculation (MED) 66 t/h / 1.1 bar / 102 °C (2) steam requirement (MED) 66 t/h / 1.1 bar / 157 °C (1)

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SLIDE 18

Dr.-Ing. Claudia Werner

Interfaces Desalination Plant - CCGT Power Station

Interface Desalination Plant Interface Desalination Plant Interfaces Desalination Plant Interfaces Desalination Plant

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SLIDE 19
  • 4. RECENT RESEARCH -

Aspects of Thermoeconomics

component k

in , k , n

C

  • in

, k , 2

C

  • OM

k CI k k

Z Z Z

  • +

=

1

  • ut

, k , 2

C

  • ut

, k , 1

C

  • 2

1

  • ut

, k , m

C

  • m

n 2

in , k , 1

C

  • Dr.-Ing. Claudia Werner

j j j j j j

e m c E c C ⋅ ⋅ = ⋅ =

  • (

) ( )

∑ ∑

= =

⋅ = + + ⋅

m j

  • ut

k j j OM k CI k n j in k j j

E c Z Z E c

1 , 1 ,

  • Source: A. Bejan, et al.: Thermal design and optimization, 1996
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SLIDE 20

ED/ED,max in % (Z/ED)/(Z/ED)max in % medium low high low medium high

  • 4. RECENT RESEARCH -

Optimisation Approach according to Ogriseck/Meyer

. . . . Dr.-Ing. Claudia Werner

An increase of the capital cost of these components is recommended A decrease of the capital cost

  • f these

components is recommended

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SLIDE 21
  • 4. RECENT RESEARCH -

Optimisation Approachaccording to Scheffler

. . . . Dr.-Ing. Claudia Werner

Direction and extent specifications for the input parameter variations within the optimisation process Example of an isoline illustration to describe the nonlinear correlation of the input parameters (x1, x2 - cp. figure)

Source: E. Scheffler: Statistische Versuchsplanung und -auswertung, 1997.

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SLIDE 22
  • 5. SIMULATION/OPTIMISATION PROCESS

Combination of the parameters of both subsystems Stationary nominal operation of the cogeneration system Simulation of the energy supply of the hybrid desalination plant

  • n the basis of GE Energy - GateCycle

Thermoeconomic analyses on the basis GATEX, MATLAB and Microsoft Excel SOFTWARE APPLICATIONS:

Dr.-Ing. Claudia Werner

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SLIDE 23
  • 5. SIMULATION PROCESS

Dr.-Ing. Claudia Werner

Electricity cost: 4.32 ct/kWh Water cost: 2.08 EUR/m³

33 67 100 33 67 100 ED/ED,max in % (Zk/ED)/(Zk/ED)max in %

medium low high low medium high CMB1/CMB2 HPSHT3/HPSH23 PUMP2 PUMP3 MPECO/MPECO2 ST2 ST1 PUMP1 MPZHT2/MPZH22

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SLIDE 24

6.RESULTS OF THE SIMULATION PROCESS

Dr.-Ing. Claudia Werner

100 °C 140 °C 1220 °C 1220 °C

  • 0.22 %

± 0.00 % Exergy efficiency

  • 0.03 %

± 0.00 % Electricity cost

  • 0.07 %

± 0.00 % CMB1/CMB2

Fuel preheating Outlet Temperature

Water cost

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SLIDE 25

Dr.-Ing. Claudia Werner

  • 0.01 %

± 0.00 % ± 0.00 % ± 0.00 % ± 0.00 % ± 0.00 %

  • 0.02 %

± 0.00 %

  • 0.02 %

85.0 % 80.5 % 85.0 % 85.0 % 85.0 % 83.0 % PUMP1 PUMP2 PUMP3

Isentropic efficiency

25.3 K 54.3 K 9.8 K 67.8 K 33.9 K 81.9 K 85.0 % 82.0 % 89.0 % 87.5 % 100 °C 140 °C 1220 °C 1220 °C

  • 0.10 %

± 0.00 %

  • 1.31 %
  • 0.20 %
  • 0.12 %
  • 0.22 %

± 0.00 % Exergy efficiency

  • 0.58 %
  • 0.43 %
  • 1.01 %
  • 0.03 %
  • 0.03 %
  • 0.03 %

± 0.00 % Electricity cost

  • 0.07 %

± 0.00 % CMB1/CMB2

Fuel preheating Outlet Temperature

  • 0.04 %
  • 0.01 %

ST1 ST2

Isentropic efficiency

  • 0.34 %
  • 0.37 %
  • 0.41 %

HPSHT3/HPSH23 MPECO/MPECO2 MPZHT2/MPZHT22

Temperature difference

Water cost

6.RESULTS OF THE SIMULATION PROCESS

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SLIDE 26

6.RESULTS OF THE SIMULATION PROCESS

Dr.-Ing. Claudia Werner

Electricity cost: 4.23 ct/kWh Water cost: 2.05 EUR/m³

33 67 100 33 67 100 ED/ED,max in % (Zk/ED)/(Zk/ED)max in % prior to optimisation after optimistion medium low high low medium high

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SLIDE 27

Application of combined methods including thermoeconomic and statistical approaches Investigation of further cogeneration concepts, e. g. combined production of hydrogen and electricity

  • 7. CONCLUSION AND OUTLOOK

Each component is characterised by specific dimensioning parameters, which qualify the relative exergy destruction and the specific cost ratios According to the optimisation approach by Ogriseck/Meyer different components are determined to affect the exergy or cost efficiency Modifications investigated result in decreased product cost (electricity/water) and decreased exergy efficiency

Dr.-Ing. Claudia Werner

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SLIDE 28

The author gratefully acknowledge the support of the Kraftwerksschule Essen e.V. and Siemens AG.

Contact Data: Dr.-Ing. Claudia Werner Technische Universität Berlin Institut für Prozess- und Verfahrenstechnik Fachgebiet: Anlagen- und Sicherheitstechnik (TK-01) Straße des 17. Juni 135 D-10623 Berlin http://www.ast.tu-berlin.de/ claudia.werner@tu-berlin.de

Fachgebiet Anlagen- und Sicherheitstechnik

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SLIDE 29

Dr.-Ing. Claudia Werner

Sensitivity Analyses - Product Cost (Electricity/Water)

Variation of the component parameters ± 5 % (prior to optimisation)

  • 0.5

0.0 0.5 1.0 1.5

  • 5
  • 2.5

2.5 5 parameter variation in % cost variation in % CMB1/CMB2 - Fuel preheating CMB1/CMB2 - Outlet temperature PUMP1 - Isentropic efficiency PUMP2 - Isentropic efficiency PUMP3 - Isentropic efficiency ST1 - Isentropic efficiency ST2 - Isentropic efficiency HPSHT3/HPSH23 - Temperature difference MPECO/MPECO2 - Temperature difference MPZHT2/MPZH22 - Temperature difference

  • 0.5

0.0 0.5 1.0 1.5

  • 5
  • 2.5

2.5 5 parameter variation in % cost variation in %

Electricity Water (MED/RO)

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SLIDE 30

Dr.-Ing. Claudia Werner

Economic Aspects of Hybrid Desalination Plants (MED:RO)

Water cost in EUR/m³ related to the ratio of MED :RO and the total desalination capacity

0.0 0.1 0.3 0.4 0.7 1.0 1.5 2.3 4.0 9.0 13500 20250 27000 33750 40500 47250 54000 60750 67500 MED:RO-Verhältnis

total desalination capacity in m³/d

1.00-1.25 1.25-1.50 1.50-1.75 1.75-2.00 2.00-2.25 2.25-2.50 2.50-2.75 2.75-3.00

MED : RO Total desalination capacity in m³/d

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SLIDE 31

Dr.-Ing. Claudia Werner

10.32 EUR/t emission certificate (CO2 ) 2.63 EUR/GJ fuel cost 1.0 % fuel escalation 0.7 % general escalation 2.3 % inflation 12 % interest rate 7446 h annual utilisation period 30 a life cycle 01/2007 reference date

Economic Data of the Desalination Plant/CCGT Plant (Selection)

Desalination data according to the publications of Wangnick Consul- ting GmbH, IDE Technologies Ltd. and A. M. Helal et al.