Systematic Analysis of Gas Turbine - Fuel Cell Combinations for Electric Power Generation with very high Efficiency. Addenda part 1

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ADDENDA

part

1

Systematic

Analysis

of

Gas

Turbine

_-

Fuel

Cell

Combinations

for

Electric

Power

Generation

with

_very

high

Efficiency

Afstudeerverslag

_van:

J.T.

Drenth

GEM()

yi

Afstudeerhoogleraar:,

Prof.

Ir.

J.

Klein

Woud

Afstudeerbegeleider:

Dr.

4r.

L.J.M.J.

Blomen

Blomeneo

B.V.

ADDENDA

CONTENTS

Addendum

A

Reformer

simulations

Addendum

B

Cycle-Tempo

description

Addendum

C

Basis

of

Design

Addendum

D

Design

H-SEL:

Heron

turbine

Addendum

E

Design

T-SEL:

Typhoon

turbine

Addendum

F

Design

L-SEL:

LM

1600

turbine

Addendum

G

Design

2HRF

10:

Heron-reformer

combination

Addendum

H

Design

3HRF10:

Heron-reformer

combination

Addendum

I

Design

2HRF13:

Heron-reformer

combination

Addendum

J

Design

TRF

1 1 :

Typhoon-Reformer

Combination

Addendum

K

Design

TRHRFI1:

Typhoon-Reheat-Reformer

Combination

Addendum

L

Design

TRHRF21:

Typhoon-Reheat-Reformer

Combination

Addendum

M

Design

LRF13:

Lm1600-Reformer

Combination

Addendum

N

Design

LRHRF

I

3:

Lm1600-Reheat-Reformer

Combination

Addendum

0

Design

LRHRF17:

Lm1600-Reheat-Reformer

Combination

Addendum

P

Design

LIRC:

Lm1600-Intercooler-Recuperator-Combination

Addendum

Q

Design

Issues

(Practical):

Figures

Belonging

to

Chapter

14

Addendum

R

Options

for

Fuel

Cell

Integration

Addendum

S

Design

TAF62:

Typhoon-AFC

Combination

Addendum

T

Design

HSP62:

Heron-SPFC

Combination

Addendum

U

Design

TSP82:

Typhoon-SPFC

Combination

Addendum

V

Design

HPA65:

Heron-PAFC

Combination

Addendum

W

Design

TPA82:

Typhoon-PAFC

Combination

Addendum

X

Design

LPA66:

Lm1600-PAFC

Combination

Addendum

Y

Design

TIM

1:

Typhoon-IR

MCFC

Combination

Addendum

Z

Design

LIM1:

Lm1600-IR

MCFC

Combination

Addendum

AA

Design

HS00151:

Heron-IR

SOFC

Combination

Addendum

AB

Design

TRCSOIR3:

Typhoon-IR

SOFC

Combination

Addendum

AC

Design

LIRCS013:

LM1600-IR

SOFC

Combination

Addendum

AD

Design

TRFS0094:

Typhoon-ER

SOFC

Combination

#1

Addendum

AE

Design

TRFS0061:

Typhoon-ER

SOFC

Combination

#2

Addendum

AF

Design

LRFS0101:

LM1600-ER

SOFC

Combination

Addendum

AG

Design

Model

63:

IR-SOFC

with

Heat

Exchange

Addendum

AH

Cost

Estimate

Typhoon

AFC

(Design

TAF62)

Addendum

Al

Cost

Estimate

Heron-SPFC

(Design

HSP62)

Addendum

Ad

Cost

Estimate

Typhoon

SPFC

(Design

TSP82)

Addendum

AK

Cost

Estimate

Heron-PAFC

(Design

HPA65)

Addendum

AL

Cost

Estimate

Typhoon-PAFC

(Design

TPA82)

Addendum

AM

Cost

Estimate

LM1600-PAFC

(Design

LPA66)

Addendum

AN

Cost

Estimate

Heron-SOFC

(Design

HS00151)

Addendum

AO

Cost

Estimate

Typhoon-ER

SOFC

(Design

TRFS0061)

Addendum

AP

Cost

Estimate

Typhoon-IR

SOFC

(Design

TRCSOIR3)

Addendum

AQ

Cost

Estimate

LM1600-IR

SOFC

(Design

LIRS013)

The

tables

show

the

numeric

output

of

Dutch

Natural

Gas

(DNG)

feed

reformer

simulations

that

_were

carried

_out

with

Cycle-Tempo's

reformer

model

and

with

another

reformer

model

(ref.bas)

which

Blomenco

B.V.

possesses.

It

_can

be

_seen

that

for

both

reformer

models

three

complete

simulation

_runs

_were

performed

for

increasing

reaction

_pressures

(1.013

bar,

7.5

bar

and

15.0

bar).

For

all

three

reaction

_pressures

the

Steam

to

Carbon

ratio

and

the

reaction

temperature

was

varied

within

ranges

that

are

most

likely

to

occur

for

gas

turbine

reformer

combinations.

For

the

ref.bas

reformer

model

both

the

shift

approach

and

the

reforming

approach

temperatures

can

be

specified.

These

temperatures

indicate

the

effectiveness

of

the

catalyst

bed

since

this

specifies

the

difference

between

the

actual

_gas

temperature

and

the

temperature

at

which

the

actual

effluent

_gas

composition

would

be

_at

equilibrium.

The

Cycle-Tempo

reformer

model

does

not

allow

such

specifications.

Therefore,

the

ref.bas

model

approaches

_to

equilibrium

have

been

set

at

1.0

C

for

the

shift

approach

and

-1.0

C

for

the

reformer

approach,

RFCTH21B.XL5

Reformer simulation from Cycle-Tempo

DNG; 1.013bar

%H2 wet

S/C= 2

S/C

=

3

S/C =4

S/C =5

S/C

=

6

S/C =7

SIC

=

8

Temperature

S/F

=

1.75

S/F =2.62

S/F

=

3.49

S/F

=

4.36

S/F

=

5.24

S/F

=

6.11

S/F

=

6.98

degr. C

600

50,90%

48,70%

45,49%

42,06%

38,75%

35,71%

33,00%

640

55,96%

52,21%

47,65%

43,28%

39,38%

36,01%

33,11%

680

59,26%

53,79%

48,26%

43,42%

39,33%

35,87%

32,95%

720

60,84%

54,12%

48,15%

43,17%

39,05%

35,60%

32,70%

760

61,29%

53,92%

47,80%

42,81%

38,71%

35,30%

32,43%

800

61,24%

53,56%

47,40%

42,44%

38,38%

35,01%

32,17%

840

61,02%

51,38%

47,01%

42,08%

38,05%

34,72%

31,92%

%H2 dry

(= %H2/(1-%H20))

Temperature

S/C= 2

S/C= 3

S/C

=

4

S/C

=

5

S/C= 6

SIC

=

7

S/C= 8

degr. C

S/F

=

1.75

S/F =2.62

S/F

=

3.49

S/F

=

4.36

S/F

=

5.24

S/F

=

6.11

S/F

=

6.98

600

65,94%

70,41%

72,82%

74,22%

75,04%

75,56%

75,90%

640

69,27%

72,59%

74,16%

75,01%

75,48%

75,79%

75,99%

680

71,38%

73,59%

74,60%

75,16%

75,52%

75,74%

75,94%

720

72,42%

73,89%

74,64%

75,08%

75,40%

75,66%

75,80%

760

72,78%

73,89%

74,52%

74,93%

75,24%

75,46%

75,65%

800

72,85%

73,78%

74,36%

74,78%

75,08%

74,84%

75,50%

840

72,82%

71,15%

74,21%

74,62%

74,92%

75,15%

75,35%

Reformer simulation from Cycle-Tempo

I

I I

ii

_

---NG; 7'.5bar

---r`Voll2 wet

(I ,r

_

Temperature

S/C

=

2 -1 S/C

=

3

S/C

=

4

S/C

=

5

S/C

=

6

S/C

=

7

SIC

=

8

ae r. C

S/F

=

175 S/F

=

2,62

S/F

=

3.49

S/F

=

4:36

S/F

=

5.24

S/F

=

6.11

S/F

=

6.98

600

31.08%

30.69%

29.82%

28.81%

27.76%

26.72%

25.69%

640

36.78%

36.05%

34.74%

33.26%31.74%

30.23%

28.76%

680

42.39%

141.11%

39.16%

37.03%

34.87%

32.78%

30.78%

720

47.59%

45.48%

42.65%

39.70%

36.84%

34.18%

31 .769-7O

760

52.06%

48.80%

44.93%

41.16%

37.74%

34.71%

32.05%

800

55.50%

50.88%'

46.06%

41.71%

37.96%

34.76%

32.01%

840

57.80%

51.90%

46.41%LI

41.76%

37.88%

34.62%

31.85%

H

13/01-12 dr (

=

%H2/(1-%H20))

Temperatur

S/C =2

_

S/C =3

S/C =4

SIC

=

5

S/C

=

6

SIC =7

S/C =8

degr. C

iiS/F

=

11.75

S/F

=

2.62

S/F

3.49

S/F

4.36

S/F

=

5.24

S/F

=

6.11

S/F e- 6.98

II

600'

50.14%

56.67%

61.06%'

64.25%

66.67%

68.57%

70.04%

640

55.50%

61.52%

65A-2%

68.16%

70.14%

71.64%

72.77%

680

60.15%

65.55%

68.86%

71.06%

72.57%

73.63%

74.37%

720

64.08%

68.67%

71.30%

72.94%

73.98%

74.66%

75.14%

760

67.20%

70.89%

72.82%

73.92%

74.61%

75.08%

75.38%

800

69.48%

72.23%

73.58%

74.32%

74,80%

75.14%

75.37%

840

w__ 70.96%

72.92%

73.85%

74.41%

74.80%

75.10%.

75.30%

=

=

Reformer simulation from Cycle-Temp

IMP; 115.0bar

Temperature

de r. C

j

S/C =2

S/F = 1.75

S/C-a 3

S/F = 2.62

S/C = 5

S/F = 4.36

%H2 wet

I

S/C = 4

S/F = 3.49,

S/C = 6

S/F = 5.24

SIC = 7

S/F -= 6.11

S/C =8

S/F =6.98

800

840

Temperature

degr. C

49.80%

53.40%

S/F =1.75

43.84%

49.30%

54.31%

46.94%

49.35%

44.98%

50.48%

55.76%

60.37%

43.51%;

40.10%

6H2 dry

(= %H2/(1-%H20))

55.19%

60.18%

64.37%

40.94%

58.78%

63.40%

67.18%

36.94%

37.39%

S/C=6

S/F .5,24

34.31%

61.57%

63.79%

65.65%

65.88%

67.83%

69.36%

69.28%

70.84%

72.06%

71.64%

72.92%

73.79%

73.31%

74.13%

74.75%

74.i3%.

75.07%

74.48%

74.88%75.l7%

34.10%

31.58%

31.66%

600

640

680

S/C = 7

S/C=8

S/F = 6.11

S/F =6.98

720

40.51%

39.32%

.57.55%

35.62%

33.63%

31.77%

29.96%

760

45.43%

43.53%

41.01%,

38.36%

35.79%

3336%3112%

25.04%

24.85%

24728-62:

23.61%

22.91%

22.21%

21.54%

30.11%

29.72%

28.88%

27.91%

26.92%

25.94%

24.97%

35.33%

34.62%

33.40%

32.02%

30.62%

29.23%

27.88%

720

58.77%

64.27%

67.74%

70.09%

760

62.64%

67,44%

70.28%

72.09%

800

65.80%

69.80%

72.01%

73.31%

840

68.25%,

71:3.9%

72.98%

73.90%

SIC =2

S/C

=

3

S/C

=

4

S/C= 5

S/F

=

2.62

S/F

=

3.49

S/F

=

4.36

600

640

680

Reformer simulation from REF.BAS

SHIFT APPROACH

=

1.0 deg C

DNG; 1.013bar

%H2 wet

REFORMING APPROACH

=

-1.0 deg C

1

Temperature

S/C=2

S/C= 3

S/C= 4

S/C

=

5

S/C=6

S/C=7

S/C= 8

degr. C

S/F

=

1.75

S/F

=

2.62

S/F

=

3.49

S/F

=

4.36

S/F

=

5.24

S/F

=

6.11

S/F

=

6.98

600

50.38%

48.20%

45.06%

41.72%

38.48%

35.51%

32.84%

640

55.50%

51.75%

47.27%

42.97%

39.15%

35.83%

32.96%

680

58.40%

53.14%

47.78%

43.06%

39.05%

35.65%

32.76%

720

60.45%

53.69%

47.76%

42.84%

38.77%

35.37%

32.50%

760

60.90%

53.48%

47.39%

42.45%

38.40%

35.03%

32.20%

800

60.84%

53.10%

46.96%

42.04%

38.03%

34.70°k

31.90%

840

60.62%

52.70%

46.54%

41.65%

37.67%

34.38%

31.61%

%H2 dry

(= %H21(1-%H20))

Temperature

S/C=2

S/C=3

S/C= 4

S/C= 5

SIC =6

S/C= 7

SIC =8

degr. C

S/F

=

1.75

S/F

=

2.62

S/F

=

3.49

S/F

=

4.36

S/F

=

5.24

S/F

=

6.11

S/F

=

6.98

600

65.64%

70.13%

72.58%

74.01%

74.88%

75.42%

75.78%

640

69.06%

72.38 Ok

73.98%

74.84%

75.35%

75.67%

75.90%

680

70.95%

73.29%

74.37%

74.97%

75.35%

75.61%

75.80%

720

72.27%

73.72%

74.46%

74.92%

75.24%

75.48%

75.66%

760

72.65%

73.71%

74.33%

74.75%

75.07%

75.30%

75.49%

800

72.71%

73.60%

74.17%

74.58%

74.88%

75.12%

75.32%

840

72.67%

73.46%

74.00%

74.40%

74.71%

74.95%

75.15%

Reformer simulation from REF.BAS

SHIFT APPROACH= 1.0 deg C

DNG; 7.5bar

%H2 wet

REFORMING APPROACH =-1.0 deg C

I

Temperature

S/C

=

2

SIC

=

3

SIC

=

4

S/C= 5

S/C

=

6

S/C= 7

SIC =8

degr. C

S/F= 1.75

S/F= 2.62

S/F

=

3.49

S/F =4.36

S/F =5.24 S/F= 6.11

S/F

=

6.98

600

30.54%

30.16%

29.31%

28.33(Y

27.31%

26.30%

25.31%

640

36.19%

35.47%

34.19%

32.75%

31.28%

29.82%

28.40%

680

41.79%

40.51%

38.60%

36.52%

34.43%

32.40%

30.47%

720

47.01%

44.89%

42.11%

39.23%

36.44%

33.85%

31.49%

760

51.52%

48.24%

44.42%

40.72%

37.36%

34.39%

31.79%

800

55.00%

50.35%

45.56%

41.28%

37.59%

34.43%

31.73%

840

57.34%

51.38%

45.92%

41.32%

37.48%

34.27%

31.54%

%H2 dry

(

=

%H2/(1-%H20 ))

Temperature

SIC =2

S/C= 3

SIC

=

4

SIC

=

5

S/C =6

SIC

=

7

S/C =8

degr. C

S/F

=

1.75

S/F= 2.62

SF =

3.49

S/F

=

4.36

S/F =5.24 S/F= 6.11

S/F

=

6.98

600

49.68%

56.14%

60.55%

63.77%

66.22%

68.13°h

69.66%

640

55.01%

61.04%

64.98%

67.75%

69.78%

71.30%

72.46%

680

59.73%

65.12%

68.47%

70.70%

72.26%

73.35%

74.14%

720

63.73%

68.33%

70.99%

72.64%

73.72%

74.44%

74.94%

760

66.92%

70.60%

72.55%

73.68%

74.39%

74.87%

75.19%

800

69.25%

71.99%

73.33%

74.11%

74.60%

74.94%

75.19%

840

70.77%

72.69%

73.63%

74.19%

74.58%

74.87%

75.10%

Reformer simulation from REF.BAS

_i

II

I

SHIFT APPROACH =1.0 deg C

DNGL15 bar

j°kH2 wet

(=H2/total)'

REFORMING APPROACH =-1.0 deg C

Temperature

S/C

2

S/C

=

3

S/C

=

4

S/C

=

5

SIC =6

S/C

=

7

S/C

=

8

egr: C

600

24.56%

24.37%

23.81%

23.16%

22.489

21.81%

21.16%

640

29.5596

29.16%

28.35%

27.41%

26.45%

25.50%

24.57%

680

34.59%

34.02%

32,82%

31.49%

30.13%

28.79%

27.48 k

720L

39.89%

38.70%

36.96%

35.07%

33.19%

31.35%

29.60%

760

44.82%

42.91%

40.43%

37.84%

35,33%

32.97%

30.79%

800

49.23%

46.34%

42.94%

39.60%

36.51%

33.73%

31.27%

ii

840

52.87%

48 :78%

44.44%

40.46%

36.97 °k

33.94% -- 31.33%

I

_

%H2 dry

r H2/(total H20))

I

temperature

181C

=

2

S/C

=

3

S/C= 4

SIC =5

SIC =i6

S/C

=

7

S/C

=

8

deur. C

I

600

43.27%

49.90%

154.63%

58.21%

61.02%

63.30%

65.17%

640

48.75%

55.20%

59.64%

62.90%

65.40%

67.37% II6sS5°/o

680

53.57%

59.86%

63.88%

66.74%

68.85%

70.46%

71.71%

720

58.32%

63.83%

67.32%

69.69%

71.38%

72.60%

-73.50%

760

62.25%

67.05%

69.92%

7137%

72.99%

73.86%

74.46%

800

65.49%

69.48%

71.69%

73.03%

73.88%

74.45%

74.85%

i

840

68.00%

71.12%

72.72%

73.65%,

74.24%

74165%

74.94%

(

The

_computer

_programme

Cycle-Tempo

has been

co-developedl

by

the

Delft

University

of

Technology

and

the

TNO

Institute

of

Environmental

and

Energy

Technology

in

Apeldoorn,

The

Netherlands,

for

computing

mass

flows,

thermodynamic

variables,

chemical

equilibrium

and

composition

of

mixed

flows

for

the

following

_processes

_or

combination

of

processes:

IL,

Steam/water

cycles

Gas

turbine

cycles

Potassium

_upstream

_systems

Fuel

cell

systems

Fuel

gasification

_systems

Freon

cooling

cycles

Absorption

cooling

cycles,

The

computer

program

can be used

for

a

variety

of

purposes.

Firstly,

_process

variables

for

_new

units

_can be

computed

and

optimised

Secondly,

the consequences

of

a

change

in

operation

for

existing

production

units,

_e.g.

related

to

the

thermal'

efficiecy,

_can be

computed.

Finally,

the

_computer

_program

can be used

for

the

evaluation

and

testing

of

results.

Input

descrIption

An

input

dataset

for

Cycle-Tempo

is

always

based

_on

_a process scheme

of

the

system

to

be

examined.

Since

this

scheme _may

only

include

apparatus

for

which

Cycle-Tempo

can

perform

calculations,

this

(Cycle-)

scheme

_may

differ

somewhat

from

the

normal

_process schemes

within

_a

particular

discipline.

When

setting

_up an

input

dataset, alb

apparatus,

piping

and

independent

cycles

are

numbered.

The

numbering

of

apparatus and

piping

is

not

tied

to

strict

rules;

the

numbers

do

not

have

to

be

sequential,

but

should

preferably

not

consist

of

more

than

three

digits.

The

identification

numbers

of

the

'independent'

cycles

should

on,

the

other

hand be

consecutive

starting

with

number

lc

In

the

input

description

of

Cycle-Tempo

a

distinction

is

made

between

groups,

indicated

by

Roman

numerals.

For

this

specific

study

of

_gas

turbine

and

fuel

cell

combination

_systems

operating

under

design load

conditions

we

used

the

following

groups.

Of: header

card,

description

of

the

problem

&CYCLE,

_parameters

describing

the

size

of

the

problem

&SYSTEM,

specification

of

the

_system

_types

&APDATA,

specification

of

apparatus

data

iV:

specification

of

the

topology

of

the process scheme.

&MEDIUM.

specifiation

of

mediumtypes

and

compositions

VI.

&EXCOND,

additional

input

data

for

pipes

(extra

condition)

VII:

&GENDAT,

specification

of

generator

data

IIX:

&TDP,

specification

of

turbine

driven

pumps/compressors

In

the

input

extensive

_use

is

made

of

the

so-called

NAMELIST.

By

using

this

facility

only

the

relevant

input

data

have

to

be

specified

and

the

user

is

given

great

freedom

with

respect

to

the

order

of

input.

Each

NAMEL1ST

begins

with

_an

identification

(e.g.

&CYCLE

_or

&APDATA)

and

ends

with

&END.

In

each

NAMELIST

a

value

can

be

allocated

to

different

variables.

All

the

input

data

together

_are

included

in _an

input

file

and

must

be

coupled

to

the

program

for

a

'run'.

Group

0:

Ileader

card

In

the

first

line

of

each

dataset

a

description

of

the

problem

_can

be

given.

This

text

then

appears

on

each

output

page

as

the

heading.

In

this

study

all

models

have

been

given

relevant

codes

in

order

not

to

confuse

the

different

combination

possibilities.

The

employed

coding

_system

is

explained

in

Chapter

8:

Design

matrix

#1.

Group

I:

&CYCLE

In

this

NAMELIST

&CYCLE

the

problem

size

is

established

by

specifying

the

following

variables:

NAPP

number

of

_apparatus

NUN

number

of

pipes

NCYCLE

number

of

'independent

cycles

(open

_or

closed)

NTURB

number

of

turbines

NTDP

number

of

turbine

driven

pumps/compressors

NPRODFUN

number

of

_user

defined

_energy

equations

NUMGEN

number

of

_generators

NUMHX

number

of

heat

exchangers

NUMGEO

number

of

apparatus

indicated

in

&GEODAT

NPRINT

this

code

determines

the

size

of

the

output

NXXX

output

control

mode

for

testing

Group

II:

&SYSTEM

In

this

_group,

for

each

cycle

_one

must

specify

whether

it

is

_an

_open

_or

_a

closed

system

by

entering

the

values

'OPEN'

_or

'CLOSED'

in

the

order

of

the

cycle

numbering.

GROUP

III:

&APDATA

Groups

III

and

IV

form

the

two

distinguished

steps

in

which

the

_system

modelling

_process

is

First

the

basic

Cycle-Tempo

elements

will

be

shown

and

the

_most

_common

_parameters

will

be

given.

Then

the

_most

important

elements

for

this

specific

study

will

be

discussed

in

more

detail.

For

the

modelling

with

Cycle-Tempo

_one

_can

choose

out

of

a

number

of

basic

system

Library of system elements

Types 17, 18, 20, 21, 22, 23, 25, 26, 27, 28 and 29 not available in commercial version

Figure

1

Library

of

_system

elements

in

Cycle-Tempo

TYPE 1: BOILER TYPE 2: REHEATER TYPE 3: TURBINE _{TYPE 4:}

CONDENSER

+

TYPE 6/12 HEATEX- CHANGER TYPE 7: TYPES: 5: F.W. TYPE 8: PUMP HEATER _DEAERATOR TYPE 9/11: JUNCTION/

SPUTTER TYPE 'Jo: SINK/SOURCE TYPE 13: COMBUSTOR TYPE 14: VALVE/

SPUTTER

TYPE 20: REFORMER

DRUM TYPE 17: ABSORBER TYPE 18: REGENERATOR

TYPE 15: MOIST. CONDENSER SEP./

0

TYPE 25: SCRUBBER . TYPE 22: FLUE GAS , TYPE 23: GASIFIER TYPE 21: FUELCELL

TYPE 26: SEPARATOR TYPE 27:

"at--@"--

TYPE 29: COMPRESSOR I V SATURATOR REACTOR TYPE 28:

In

order

to

make

this

section

not

too

laborious,

only

the

most

common

paramaters

and

thermodynamic

data

for

these

_apparatus

_are

specified:

NO

_apparatus

number

TYPE

_type

code

for

_apparatus

(see

Figure

1)

MEDNR

cycle

number

to

which

the

primary

(=heated)

medium

belongs

PIN

inlet

_pressure

(bar)

POUT

outlet

_pressure

(bar)

DELP

_pressure

loss

in

the

_apparatus

(bar)

TIN

inlet

_temperature

(C)

TOUT

outlet

_temperature

(C)

Types

1-15

of

Figure

1

have

been

developed

for

conventional

steam-

and

gas

turbine

cycles.

Types

17

and

18

_are

_system

elements

for

absorption

heat

pumps.

For

the

analysis

of

fuel

cell

systems

types

20-22

_can

be

used

and

for

integrated

coal

gasification

combined

cycle

_systems

types

24-28.

Most

important

for

_our

system

study

_are

the

following

elements:

turbine

(type

3),

combustor

(type

13).

reformer

(type

20).

fuel

cell

(type

21),

moisture

_separator

(type

22),

separator

(type

26)

and

a

reactor

(type

27).

A

short

description

of

the

main

characteristics

of

each

of

these

types

will

be

given

below.

Turbine

(type

3)

This

_apparatus

_can

be

used

_to

model

_an

expansion

_process,

irrespective

of

the

medium

expanding

in

the

turbine.

Each

turbine

can,

in

addition

to

an

inlet

and

an

outlet

_,

have

a

maximum

of

8

extractions.

The

addition

of

_an

extra

massflow

in

the

expansion

section

between

the

turbine

inlet

and

outlet

is

not

possible;

in

this

_case

the

turbine

can

be

modelled

as

two

turbines

in

series.

(*

_see

also

the

section

6.3.2

of

the

final

report

text:

Modelling

problems

and

solutions)

The

turbines

and

turbine

sections

distinguished

by

the

_programme

_can

be

classified

in

two

categories,

indicated

by

the

turbine

code

TUCODE:

General

turbines

TUCODE

₌

0

Specific

steam

turbines

TUCODE=

1

-9

The

general

turbine

_type

_can

be

used

_as

a

steam

turbine,

but

is

more

intended

as

an

expansion

section

of

a

gas

turbine

installation,

and

as

a

turbine

type

for

various

media.

For

this

type

no

routines

are

available

for

determination

of

the

internal

efficiencies;

these

must

be

specified

either

directly

or

indirectly.

No

exhaust

losses

_are

computed

for

this

_type

either.

Several

types

are

available

for

modelling

steam

turbines:

turbine

code

TUCODE=

1

_-

9.

By

using

these

_types

_a

turbine

of

virtually

_any

size

_can

be

modelled.

The

internal

efficiencies

do

not

have

to

be

specified

because

for

all

these

types

procedures

to

calculate

this

_are

incorporated.

The

exhaust

losses

_are

also

determined

and

_are

balanced

with

the

computed

It

should

be

noted

that

the

method

for

calculating

the

efficiencies,

which

is

based

_on

data

from

General

Electric,

dates

from

1974

and

that

the

Cycle-Tempo

manual

indicates

that

with

_present

day

_steam

turbines

_greater

efficiencies

_can

be

obtained.

It

is

for

this

_reason

that,

although

the

incorporated

steam

turbine

_types

_may

be

_very

useful

for

tendency

calculations,

_we

have

decided

to

use

the

general

turbine

type

in

_our

calculations,

i.e.

by

specifying

TUCODE=0,

since

it is

_our

design

philosophy

_to

maximise

the

efficiency

of

electricity

generation.

This

implies

that

assumptions

for

the

internal

efficiencies

of

_steam

turbines

had

to

be

made.

These

assumptions

are

specified

in

the

_next

addendum:

Definition

Basis

of

Design.

Heat

exchanger

(type

6

or

type

12)

The

difference

between

these

two

types

of

heat

exchangers

is

that

in

_a

type

6

heat

exchanger

the

_energy

balance

is

used

to

compute

the

specific

enthalpy

at

one

of

the

inlets

or

outlets,

whereas

in a

type

12

the

energy

equation

is

used

to

compute

the

mass

flows.

For

the

latter,

a

user

defined

energy

equation

must

be

specified.

The

_temperature

determination

for

heat

exchangers

is

pictured

below.

Figure

2

Temperature

determination

heat

exchanger

It

follows

from

this

figure

that

both

counter

flow

and

parallel

flow

_can

be

modelled.

(Unless

stated

otherwise

the

heat

exchangers

modelled

throughout

this

report

will

be

of

the

counter

flow

type.)

TIN

and

TOUT

refer

_to

the

inlet-

and

outlet

_temperature

respectively.

The

digits

1

and

2

indicate

whether

a

stream

is

heated

up

or

cooled

down.

The

variables

DELTL

and

DELTH

are

important

for

a

good

understanding

of

Cycle-Tempo's

output

files

and

refer

to

the

low-

and

the

high

terminal

_temperature

differrence.

Combustor

(type13)

In

the

combustor

an

oxidant

and

a

fuel

flow

react

to

chemical

equilibrium

at

specified

or

at

computed

conditions.

Although

under

actual

conditions

the

reactions

will

not

run

to

was

thought

to

be

meaningless

because the

degree

_to

which

the

initial

composition

differs

from

the

equilibrium

composition

is

determined

by

factors

which

depend on

the

design

of

the

combustor.

Radiation

losses

_must

be

specified

by

using

DELE,

i.e.

the

_energy

flow

_to

the

environment

(kEs),

because _no heat

transferring

_area is

_modelled

in

the

combustor:

The

heat

which

is

released is used to increase the

temperature

of

the

flue

_gas and

ash.The

reaction

enthalpy

is

computed

and is used in the

_energy

balance.

Depending

_on the

specified

_energy

equation

code

(EEQCOD)

there

are

two

possible

_ways

of

using

the

_energy

balance:

The

_energy

balance _can be used

_to

define

_a

massflow

(EEQCOD

=1).

The

energy

balance can be used

to

define

the

temperature

of

the

outgoing

flue

gas

(EEQCOD

= 2).

The

composition

in the

incoming

lines

(fuel

and

oxidant)

must

always

be

specified,

_or

computed

in

the

_apparatus

_upstream

in

the

_process

scheme.

The

composition

in

the

flue

_gas

duct

is,

_as said

before,

computed

according

_to

chemical

equilibrium.

The

temperature

and

the

_pressure

_at

which

the

chemical

equilibrium

is

computed

can be

determined

by

specifying

TREACT

and

PREACT

respectively.

Reformer

(type

20)

The

reformer

model

determines

the

equilibrium

composition

of

the

product

_gas based

_on:

Fuel

composition

Prescribed

reaction

conditions:

reaction

temperature

(TREACT)

and

reaction

Pressure

(PREACT)

Steam _to

fuel

ratio

(SFRATI)

(*

Throughout

this

study

all

_partners

have used

standard

natural

_gas

(STNATGAS)

_{as a}

fuel.

This

is _a

default

composition

for

Dutch

Slochteren

gas,

which

is

available

in

Cycle-Tempo.

For

this

composition

the

ratio

between

Cycle-Tempo's

Steam-to-Fuel

ratio

(SFRATI)

and the

_more

generally

applied

Steam-to

Carbon

ratio

is ₊

/-

1.75

_:

2.0)

The

flue

_gas

outlet

_temperature

at the

secondary

side

(cooled

medium)

is

determined

based

on

the

_amount

of

heat

required

for

the

endothermic

reforming

_process

and

the

(prescribed)

temperature

increase at

the

primary

side (heated

medium).

Fuel

cell

(type

21)

Cycle

-Tempo

_now

includes

models

of

all

five

fuel

cell

types

that

_are

considered

in

this

study:

AFC,

SPFC,

PAFC,

MCFC

and

SOFC.

Before

a

more

detailed

description

is

given

of

these

models,

first

a

few

general

features are

listed:

The

model

is

1-dimensional:

For

the

calculation

of

I

(cell

current),

V

(cell

voltage)

and Pe

temperatures,

pressures and

compositions

in

a

cross-section

perpendicular

to

the

direction

of

the

fuel

flow

are assumed to be

constant.

The

model

is

isotherm:

The

calculated

chemical

equilibria

_on the

active

cellarea

as

well

as

the

current

density

are based _on the

_average

cell

temperature.

A

fuel

cell

stack consists

of

a

number

of

cells,

all

with

the

same

performance,

electrically

connected

in

series.

Although

differences

exist

between

the

different

types,

all

fuel

cell

models

in

Cycle-Tempo

_are

based _on

Figure

3.

1) anode inlet area 2) active anode area

chemical equilibrium (Treact. Preact)

current distribution

cell voltage

outlet conc. anode

't

021

C 02

outlet _conc. cathode

3) cathode

Tfcel,

Reel

Figure

3

Lay-out

fuel

cell

model

Block

1

This

calculation

block

_can be used

to

model

_a

reforming

reaction

in the

cellstack

and

will

therefore

only

be _necessary

for

internal

reforming

MCFC's

and

SOFC's.

At

the anode

inlet

_area the

fuel

will

react

to

chemical

equilibrium

at the

specified

(Treact,

Preact)

conditions.

It

is assumed that

this

_process

takes

place

at a

constant

temperature

and

that

the heat _necessary to

drive

the

endothermic

reaction

is

extracted

from

the

reactions

that

_occur

in the

fuel

cell.

Block

2

In

this

block,

which

models

the

active

cell

area, the

cell

voltage

V,

the

cell

_current

I

and the

electrical

_power

_output

Pe _are

calculated.

It

is assumed

that

the processes

take

place

at a

constant

temperature

and a

constant

pressure

that

is

the

user

specified

celtemperature

(TFCEL)

Should

all

fuel

_components

(*

Only

H2,

CO

and

CH4

_are

considered.

The

contribution

of

higher

hydrocarbons

is

neglected.

However,

the

assumption

_to

consider

CO

and

CH4

_as

fuels

for

the

AFC,

SPFC

and

PAFC

resulted

in

irrealistic

models,

_see

also

Section

6.4.2:

Modelling

problems

and

solutions.

)

be

converted

in

the

fuel

cell,

then

the

resulting

fuel

cell

_current

would

be:

0

ma 1-1

in

(y°,+

y'co+

ycH,)

ir

₌

Mm

Yoi

_are

inlet

conditions,

ma,in

is

the

ingoing

anode

massflow

and

Mma

is

the

anode

molemass.

In

practice

the

fuel

is

converted

only

partly

in

the

fuel

cell

indicated

by

the

fuel

utilisation,

Uf:

the

ratio

between

the

actual

and

the

maximum

conversion.

The

actual

cell

_current

is

the

given

by:

Besides

the

facility

_to

calculate

the

cell

_current,

this

block

also

contains

relationships

for

the

calculation

of

the

cell

voltage.

In

this

study,

however,

the

parties

involved

have

decided

to

specify

the

cell

voltage

in

the

input

list.

The

_reasons

_to

do

_so

resulted

from

practical

considerations:

1)

The

alternative

if

the

cell

voltage

is

_not

specified,

is

_to

specify

the

fuel

cell

power

output.

Especially

at

the

beginning

when

it is

likely

that

_many

changes

have

_to

be

made

in a

model

this

is

an

extremely

difficult

thing

to

do.

2)

The

next

Addendum

on

the

Basis

of

Design

will

_present

so-called

cell

voltage-current

density

_curves.

From

these

_curves

a

realistic

cell

voltage

_can

be

determined

_very

easily

for

different

operating

conditions

The

generated

electrical

_power

equals:

Pc, ₌ V I ₇₁

.ACDC

in

which

hacdc

_accounts

for

the

dc/ac

conversion

efficiency.

This

block

also

calculates

the

composition

at

the

anode

outlet.

Based

_upon

Faraday's

law

the

amount

of

H2

and

CO

that

is

converted

_on

the

cell

is

determined.

The

assumptions

_on

which

this

calculation

is

based

depend

_on

the

selected

fuel

cell

_type.

For

high

temperature

internal

reforming

fuel

cells

it

is

assumed

that

both

the

shift-

and

the

reforming

reaction

_run

_to

equilibrium

_on

the

electrode

surface

_at

the

specified

celtemperature

and

celpressure.

For

high

temperature

external

reforming

fuel

cells

it

is

assumed

that

only

the

shift

reaction

proceeds

to

equilibrium

For

low

_temperature

fuel

cells

the

composition

of

the

incoming

anode

flow

forms

the

starting

point

for

calculation

of

the

anode

outlet

composition.

Both

the

shift

reaction

and

the

reforming

are

assumed

not

to

take

place.

Block

3

In

the

third

block

the

cathode

outlet

composition

is

calculated.

(1)

First

the

_{masstransport}

from

anode to

cathode

is

calculated

from

the

cellcurrent

I.

Incase

of

_an

SOFC

the

total

massflow

of

02

from

cathode

_to

anode is

given

by

Mo

₌

Mrnr,

_-

4F

The

composition

at the

cathode-exit

can

now

be

calculated

from

the

mole

balance

of

the

components

at the cathode.

When

the

three

parties

responsible

for

the

modelling

decided

to use

the

Cycle-Tempo

computer

programme

they

_were

well

_aware

of

the

fact

that

until

then

only

two

fuel

cell

_types,

namely

MCFC

and

SOFC,

_were

available

in

Cycle-Tempo.

In

other

words,

the

low

temperature

fuel

cell

models

still

had to be

developed.

This

_was

_not

_seen as

too

big

a

problem

since,

in

the

first

few

months,

the

company

who

would

do

the

low

temperature

fuel

cell/gas

turbine

simulations,

Blomenco,

would

be busy

_not

only

getting

_to

know

the

software

but

also

working

out

the gas

turbine/external

reformer

combinations

needed

for

expansion

with

AFC,

SPFC

and

PAFC.

In

this

study

only

design

calculations

are

performed.

For

the

Cycle-Tempo

input,

this

requires

specification

of

the

cell

voltage,

the

_current

density

and

the

utilisation

by

the

_user.

Based _on

these data the

cell

resistance and the

cell

area are

calculated.

Moisture

_separator

(type 22)

The

operation

of

this

_type

is _as

follows:

Incoming

_gas is

cooled

by

_a

cooling

medium

flowing

in the

opposite

direction,

as a

result

of

which

water

vapour

condenses.

The

condensate

formed

is

collected

and

discharged

via

a separate

pipe.

It

is assumed in the model that

both

the _pressures and the

temperatures

of

the

moisture

separated

and the

outgoing

_{gas are}

equal.

The

gas leaves the

separator

saturated.

Separator

(type

26)

The

physical

meaning

of

this

model

is that

of

a

separator

of

solid

particles.

In

order

to

simplify

calculations

it

is

possible

to separate any

desired

component

from

a gas

stream;

physically

this

resembles

separation

by

membranes

_as

far

as gases are

concerned.

The

keynote

has been to

give

the

user

the greatest

possible

flexibility

in

defining

what

and

how

much

components

have

to

be

separated.

As

a

result

of

this

no

protection

has been

incorporated

to

prevent

processes

that

_are

physically

impossible.

The

only

criterium

is _a

matching

mole

balance

without

chemical

reactions.

The

_energy

losses that

occur

during

the

separation

_process

_must

either

be

specified

by

the

_user

_or

follow

from

the

_energy

balance.

Reactor

(type

27)

Type

27

is

a

chemical

reactor

in

which

a

new

equilibrium

is

calculated

on

the

basis

of

an

equilibrium

temperature.

This

implies

the _use

of

equilibrium

constants

which

depend

only

upon

the

equilibrium

temperature:

Kreaction

f(Treaction)

with

Kreaction

equilibrium

constant

Treaction

equilibrium

_temperature

(K)

In

this

project.

type

27

has

been

used

to

simulate

the

CO-shift

or

watergas

shift

reaction:

CO

+

H20

CO2

+

H2

(5)

with

equation:

(aPco,±

x)

(N,

+

x)

KPS

("co

x)

(aPti,o

xi)

in

which:

dPx

₌

partial

_pressure

of

_component

_x

x

=

reaction

coordinate

of

the

water

gas

shift

reaction.

KPS=

reaction

constant

of

the

water

gas

shift

reaction

The

reaction

pressure

can

either

be

specified

(PREACT)

or

be

left

out

in

which

_case

lowest

inlet

_pressure

is

assumed

to

be

the

reaction

_pressure.

Equation

***

is _a

second

degree

_poynome

in

_x.

The

_new

gascomposition

_can

be

calculated

by

solving

the

polynome.

In

order

_to

select

the

_proper

solution

_an

algorythm

is

_present

that

verifies

the

following

_two

demands:

The

solution

must

be

real

Of

_any

substance,

the

maximum

quantity

that

reacts

may

never

exceed

the

quantity

that

is

_present.

Group

IV:

TOPOLOGY

OF

THE

PROCESS

SCHEME

In

this

part

of

the

input,

the

structure

of

the

process

scheme

is

determined.

For

each

pipe

in

the

process

schem

the

following

data

must

be

input

_as

whole

numbers:

identification

number

of

the

pipe;

number

of

the

apparatus

at

the

inlet

of

the

pipe;

number

of

the

apparatus

at

the

outlet

of

the

pipe;

pipe

code;

number

of

the

cycle

to

which

the

pipe

belongs.

The

pipe

numbering

does

_not

have

to

be

consecutive.

The

pipe

code

is

used

to

indicate

the

difference

between

primary

and

secondary

medium,

_or

_to

indicate

_a

special

relation

which

this

pipe

has

with

the

apparatus

connected:

(6)