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B

EL

1.1 1.1. ,

1.2.1 , .2.2

1.2.3 1,3.4

2.1.1

2.2.6

2.2.8

2.2.14

2.2.22

2.2.20

2.2.29

2.3.3

2.4.5

2.4.6 Duol

A~orption

Add-on Duol Absorption Using Converter Heot

Add-on Duol Absorption Udng Furnoce Heat

Add-on Duol Absorption Using Outside Heat Source

SOrS03 Convers ion Improvement

No2C03 Absorption of S02 to Produce N02S03

Mcgnesium O

x

ide Absorpt

i

on of S02 with S02

Recov~ry

Poto

s

sium Sulfite-B

i

sulfite

S02 Absorption in ond Recovery from Methylarnm

o

nium Sulfit

e

-Bi

su

lfile Solution

Absorption ond Oxidation of S02 in C

h

orcoal B

ed

s (

Su

lf

o

cid

P

rocE's

s

)

Absorption with Basic Aluminum Sulfote So

l

ution

,

R~generotion with H

eet

to

Release S02 (Hordmon-Hold

e

n)

Resin AdsorpHon of S02

Um

e

Absorption of S02

Ammonium SuHit

e

-Bi

s

ulFite Absorption with S02 R

e

covery ond NH

4N

03 Production

SuJfuric Acid-Li;-:'le 2-S

t

a

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Absorption to Recov

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r S02 ond Produc

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Plos~er of Poris

(8)

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,.,

2.4.5 Non. 2.000 or Ie ••

·

_T'"

2.4. , Non. 2. ~OO or le ••

·

_{1 "}

TABLE 9:

FEASIBlE P

ROCESSES

FOR

250 PPM S02 CONTROL EFFECTIVENESS

Li.mitat~ ot S02 Capa.ble ot Acld Maat

procoeaa Llmt~tlaru or AE:21tcation [nIet Concentrati.on EErr. ~-"j~

2. I. I Non. 6. 000 or lellM

·

o.,Uond

2.2.

e

Non. 5.000 or lea.

·

ophonal

2.2.8 None 5.000 or lesM

· ,.,

7.2.14 None 5.000 or lu.

·

Y"

2.2.22 Non. 2.800 or Ie •• T"

2.2.28 NOM Non. Y"

2.2 .• 9 None Noo. 1 "

2.3.3 None 6.000 or le .. e

· ,.,

2.4.5 None S. 000 or lei.

.

,.,

2.4.

e

None 6. OOÜ or Ie ••

.

1"

Removol and

Recovery

of Sulfur Oxides from Tail Goses

TABLE

JO:

FEASIBLE P

R

OCESSES FOR

500 PPM S02 CONTROL EFFECTIVEN

ESS

Capable of

Aci:.!

Proces~

Limitations of Applicati

e

n

Limit:>tions

of

502 lnlet Conc

e

ntr

a

tion,

pom

Mist anà

S

03 Cor:.::-

o

l

1.1. 1

1.2. 1

1.

2.2

1.

2.3 2.1. 1

2.2.6

2.2.8

2.2.14

2.2.22

2.2.28

2.2 .

29

·

2.3.3

2.4.5

2.4.6 Xew S. Burning only

Existing S. Burni'lg only

Existing S. Burning only

Existing \Vet Gas only

Xone

None

Xot

_~pplicable

None

5,500 or

less

~

None

No

Optional

Yes

Y

es

Yes

Y

es

Yes

Ye

s

(9)

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TAOlE 160: CONT

ROi..

COSTS

FO

K

VA

RI

O

U

5 DUAL

ASS

O

R

PTION P

ROCESSES A

P

LlED Ta VARIOUS

TyPES

,

CAPACITl

ES !,ND EFF

I

C

I

ENC!E

S O

F A

C

ID P

L

A

N

TS

FO,!

~

,

UÛ P!-'I

,\

SO?

CO

N!

,;CL

[,:,:cCTlVE~"c

S~

H

ft

f

j

f

H2Y

1,

7

~ 1.1.1 0...1 AbOOrpcloo(l) 1.2.1/1.1 1.2.1/1.2 1.2.2/1.1 1.2. :1./1. 2 1.2.3/1.' (2) Aboul 1510 IDlt!.>1 Eml •• io.l ~ ',000 4, 0Il0 3,000

'.000

3,200

_~~~plc'COr.'1t..aq ProdlJ.C"til'Q

1ULQ 2~O TID ~ 1.500 T/D !:2J.I.Q l>l TIO ,~c ,ID 1.5(>() TI"

, . U ,.I~ $.11

,

.

I."

1.48 3.~ 1.35 .18 2.30

.n

.~~ 1.3Q .8S .1f .13 .51 .(1 2.31

Souree:

Report

PB 190393,

Chemico (Morch

1970)

TABlE 166: CONTROL COST FOR VARIOUS TAIL GAS

RECOVERY

PROCESSES APPlIW TO VARIOUS TYPES,

CAPACITI

ES

AND

EFFICI

E

NCIES

OF ACID

PLANTS FO

R

502, 503 AND MIST

CONTROL

Emis~ion

Level

Process

In

Out

50 tpd

250 t;:>j,

750lpd

1,500

tod

2. 1. 111. 1 5, Doe ppm 250 p;>m

•

3.13 S

•

2.1.1/1.2 4,000 200 3.05 2.2. e/1. I' S,OOO 2S0 2. S7 2.2.6/1.2' 4,000 200 8.81 2.31 1.05 .U 2.2.6/1.2' 2,500 125 2.38 .2.2.6/1.2' 2.000 100 2.35 2.2.8/1.'- 3,200 160 2.70 2.2. e/l. 1 5,000 2&0 2.71 2.2.e/l.2 4.000 200 8. e2 2. SI J.18 .80

"

-

I ).2.8/1,2 .2. eoo .130 8.10 2. &1 1. 16 .18 2. J.

eli

.•

3, lCD 100 2.g2

I

(rontinucd)

2.2.8/1.1 8,000 2S0 2.14 I 2.2.8/1.2 4,000 200 2. 7~,

/

2.2.e/l.4 3,200 laO 2.3S

/1.98

~ 2.2. uIl. 1 5,000 250 2.l. 14/1.2 4,000 200

_{' / / l.aa}

1.03

.n

a.

2. uIl. 4 3,200 181) 2.58 2.2. 2S/I. I 5,000 600 2.87 2.2. 2al I. I 5,000 2~0 2.87 2.2.2e/I.2 4,000 200 2. es 2.2.29/1.1 0.000

-o-

1.50 2.2. 2v/l. 2 4.000 -0· •• 16 1. 83 1.

oa

. e.

2.3.3/1.1 ~,OOO 230 •• 33 2.3.3/I.l 4,000 200 '.00 2.H 1.33 .~ 2.3.3/1. 4 3,:100 180 2.48

1.4. S/I. 1 &.000 2~0 2.U

"2 ••. s/l.2 ~.COO 200 ~.52 2. 4. ~/,t'

.

•

3.200 UO 3. OS 2.'. GIl. 1 &,000 250 ~. ~O t. 4. 61 I. ~ ~. OVO 200 3,33 J ••• eli •• 3.200 Ito 3.1G

(

l':Ln

L

:~

·l

•

S02 f:rnl •• lon C""t",1 0,,11

(10)

, 1

r"

l

[~

[ ]

n

'"

"

TABLE

13:

APPROXltvLATE CAPITAL INVESTfv\ENT RcOUI:.!t.',,\~NiS FO~ Vi'i;IOUS s'-~.., CONTRO!...

SYSE

.'-,:;

A?FLlED

Ta 250

1"/0

H2

S0

4 PLANTS _

&'

_

Cl .... I. t !loIl/I.Ir 8101rn'''''l Cla . . t. J ~1.l"ItI RloIml.A( C'~. 1. J S",U .. r a<l",aa. Cb •• 1.4 Sa"..:","" \: ••

_ _ .~~ r:-nI •• JE!l..J...--!.L-- 1 ~Opwm~~L-- ~~.I •• I.;JOLt".\ , 7,;C· ~ t~.I! .. -:_~ _

ï:'"dd'IActd

... , AdQ üy Jo' .... .:, COi'Itrol CI.,II.l Dy t'rod. C(.~lNi C"p't..l .41014'j

At'

"

hl i'rvd . C. •• ~HrvJ C.jU\&1 AoH" Ac.\.d 1!oJ')o"t"O<l. Ç ... :('Ul C.,..l&I

~ ~ -ILL -f.!!- ~.!.L ..JlfL .JlJL ..L!L ~ ~ .J.LlL 2.!L. ~ ~ -.J.lIL- ~.!1._._~ J><!!I ~

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....

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lt.

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11) \tflth J,!:_~QI "'0<iI'~.1 S",llllr nrln,

..

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WI~o,o,.r., Ad41\.l.""",,1 a..u.t_r t"lrv.,

l

r

~\

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:

:-:::

I. ,~

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l

Removcl and

Recovery

of

Sulfur

Oxides from Tail Gases

TABLE

17:

COMPARISON OF ACID PRODUCTION CaSTS FOR MULTI-UNIT PLANT WITH CONTROL

SYSTEi\\S

1.2.1 ',ND 2.2.6

NOTE:

Plant consists of 4 units; 2 class

1. 1. 150 T /0

each

.

1 class

1.2, 300 T/D

and

1 class 1.2, 600 T/O for a

total da ily production of

1, 200 T / O

.

Process

Nominal Capacity

Production

Rate

Conv

;:,

rsion

R3te

Initial investment

Book V::!lu

e

Raw

Material and Utilities

Sulfur

EIee. Power

Cooling Water

Process Water

B. F

.

Water

Steam

FuelOi!

MgO

Operating Expt:nses

Labor

Supervis ion

Maintenance

(40/0)

Overhead

@

70'10

of Above

Indirect Costs

D~preeiation 10"/0)

Interest

7-1/2,,/0 )

Taxes and Insurance

(1-1/2')'0)

Annual Operating Cost

T/Y Acid Production

Proauction Cost/T

2.2.6/1. I, 1. 2 (1200)

1,200 T/O

l,254T/0

99.775 c;",

$6,215,000

3,295,000

$3,390,000

211,000

124,200

1,650

28,900

- 322,500

150,300

53,800

237,500

63,300

247,500

384,000

576,500

93,200

$5,239,350

413,300

$

12.68 Note: (Iass

1.) Units As

s

um

ed

5,000

ppm

Emis

sion

(Ia

ss

1.2 Units Assumed 4,000

ppm

Ernission

$ource: Report

PB

190393, Chemico

(Morch

1970)

1.2.1/1.1,1.2 (1200)

1,200 T/D

1,2~0

T/D

9

9.

5 %

$6,825,00

0

~.QSOOO

$3,390.000

277,000

144,000

1,650

23,700

- 260,000

190,000

63,300

273,000

368,500

683,000

102,300

$5.256,450

412,000

$

12.76

8

(11)

-, 1 r '

I'

I I "

,

n

1 ;

-

9 -

-<3-T

ABLE

1 4:

ESTI"'~

TED CA

PITAL

I

NVESTf,\ENT REOUIREMENTS

FOR

SE

L

ECTED SOl' tM/SS ION

CO

N

PO

:"

P\OC~SSES

AT VAR

IOUS i'LANT

CAP

..

~CITIES

Prciccs~

1.1.

1 Duol Absorption

(new plant, s

ulfur

burning)

1.2.2/1.2

Add

-

On

Duol Absorption

, 2.2.6/1.2

~O

Absorption

2.2.14/1.2

fv\ethylamin

e

S03-HS03

Abs.

2.2.29/1.2

Resin Absorption

2.3.3/1/2

Ume Absorption

Initiol

Control

Em

issi

on

Eff

e

c-L~vel

tiv

enes

s

*

50 ST

/

D

500 $

4,000

500 260,000

4,000

200 285,000

4,000

200 270,000

4 ,

000 -0-

195,000

4,000

200 180,000

Souree:

Rep

or

t

PB

190393,

Chemico

(Morch

1970)

CLEAN GAS TO STAO<

250 ST/D

$1,300,000

482,000

510,000

465,000

442,000

285,000

v

750 ST

/

D

$2,500,000

920,000

780,000

765,000

870POO

425,000

I

1

"

":

J,

r"

" • "'-' ;j .(

Figure 2.

Magnesium

base

1500ST/D

$3,700,000

1,450,000

1,045,000

1,080,000

1,312,000

570,000

·ppm

S0

2

recovery prüc

e

ss

élS

appli

ed

to

an

H

2

S0

4

plant.

9

(12)

-( ,

_{Removel end Recovery of}

_Sulfur

_{Oxides fr}

_o

_{m Teil}

_G:Jses

10 -FIGURE 155: GRAPH

SHOWING

VARIATION IN CONTROL COST

WITH PLANT

CAPACITY

IJK)WIHAL PL4.HT CAP.LCITT, ST/D

Source:

Report

PB 190393, Chemica (March 1970)

Removel end Recovery of Sulfur Oxides from Teil Geses

FIGURE 154:

GRAPH

SHOWING

VARIATION OF

COÎ~TP.Ol

COST

WITH

INLET

~02

CONCENTRATION IN rAil GAS

'1

l J

f1

[]

n

>=J

INI.CT SOl c~-.ct"IITIII ... TlOIif. 11'1'.

r'

l,

Souree:

Report

PB 1903Ç3, Chemica (Merch 1970)

(13)

(

,

r

1 l)

f1

n

11 ~_:','-~

::{\..J~

.

,

-'

~Î-

-

'

I

""'

"

. '

"

,.,

..

,

..

~

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400 500 TC "'Pé nATure;:: • c °2/S02"I.O~ COOLEO

soo

PPIJ

\

~'

\.rI~~

600

Figure

4. Th

ecrcticzd equi

librium

curve

(20)

I

l , r

L

r:

'

L

r:

fi

n

r

(

_

.

_---

-Fi[,urc

6. Typical alkyIJtion sludge acid or

H

2

S sulfurie

acid

plant.

HOC I

"'~"".

~

_

"-'~' ~~

'.:"! _ , IlOw

OO"~

1 LJ4

I'

I

-&"~'

:t«>-f~ " I 4;::0 ot..; - -. I.~~' =---=...;~ 1'10. " I ! J , 'UUUCl 10.\ . . L •• - --- - - -- - -

1 &

.

,

I fO tl_IJ .... \0.'110 .. 10"'U (ONObUU

.---I>'--'\/' ..

- - - " .

"'aouetto

"0'''''''

.''''. "'}fO ..

~V'" , ... "'.

, . OOu( I ,.

,..c

(00\"

!F

ICOC2

1~

.1

Tab.

12.

Bi/dullg I'on

SO,

aus SO.-I/lIlfigen Gasen /Ioclr Bode/lsfein IIl/d Pohl [11]

ZUS~n1nl~n::c t '1 Ing _Umsatz

_(X

_{der Th~oric)}_{b~i \'~rschjedcnen}_{TempcrJ.turcn}

des SO~-GJ.sgcmi:;chC'.:i

N,

I

SO,

I

0, _400·C

I

~OO'C

I

600·C

I

700'C

I

SOO'C

I

900'C Vol.· % Yol.·::;': _I Yol.-%

84,1l5 10,10 5,05 96,2 83,2 • 59,1

I

I 31,9 15,0 7,0 8J,OO 7,00 10,00 99,3 93,4 73,3 I I 42,5 20,5 9,8 81,40 4,CO 14,60

I

99,4 94,9 73,3

_I

48,1 24,2 11,7 30,00 2,00 !

,

18,00 99,4 95,6 80,5 51,3 26,3 12,9

I

79,00 J4,OO

I

7,00

9G,3

84,7 62,2 1 35,2 18,3 8,2 89,50 7,00 _I 3.50 I 93,2 81,2 55,5

_I

28,5 J2,9 6,0 0

_I

6(,,67

I

33,33 98,1 91,3 76,3

i

51,5 30,1 16,0 0 33,JJ 66,(,7 99,7 97,3 88,5

_I

60,6 40,4 22,0

0 I

J·I.OO

i

86,00 99,8 97,9 90,3

I

69,8 43,9 24,4

0

7,00

i

93,00 9~,3

i

98,1 90,5 70,7 44,9 25,3 0 _I 2,00 98,00 99,8

_i

98,2 90,8

I

_I 71,2 45,5 25,6

-

18

(21)

-I '

:

I

L • i '

f'

J

_,

_.

,

1 ~,

,

l

J

n

Figure

PRAP

process

for

making

suliuric

acid

from

pure

sulfur

dioxid~,

SOz

CONVERTE.R

RECYCLE

BLO

'

nER

ABSORPTION

~--7l

TOUR

COOLER

19 -PRODUCT

ACID

PARTlAL RECYCLE

A IR

P

1W

CESS. ZEER LAGE IlNESTERnrC; EI:rSSIE

6(1::)

-

7eo

ppm

SO

')

,

PURGE

LlQUID

SOz

~

______________________

~t~

______________

ST~~

~----I-OX-Y-GE-H

________________________

~~I

OXYGEIi

PLAHT

BOILER '>I:..---<-i

BOILER FEED

WATER

EXCHANGER

RECYCLE

BLOWER

COOLER

ABSORPTlGrI TOnER

PRODUCT

ACID

fir:ure

IRO"?

process

tor maki

lIg

sulfurie

acid

from

pure

sultur

dioxide.

TOTAL

R

E

CYCLE

OXYGE~J

PROCESS: DUi(F

rUURSTJFFA

BRIEK.

IFIGUUR-21I

.

~

.

"'-

... -

..

' . .,.

BOGS

DRU

K

PROCES

HOGE

rO~:'IERSrE

'53

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(22)

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EXPOSIT/EDUUR

I

DUU;,> IN P,70CEflTEN VA.V EE'.',' ..i/,,-',,7

C::> _{_ _ _ _ _ _}'.~ 0.; ' -

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r

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(23)

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FIGUUR -

23A

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VOEDINGS-~Aa QUU:~CH

LU

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Ta

rmtewiss

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TusseRbsorber

FIGUUR -

2 3B

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Aanpassing met quench

r

(25)

III

dl

UI

I]

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(26)

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r

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Function

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ENTHAL

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FN

TI

bijdrage

ENT

enthalpie-bi,idrage

RNT

ZHAVRLZUUR,

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berekening

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ENTHAL=

ENTHAL+ENT

23 -FIGUUR -

24 Invoer: Fnrmules v

oo

r de enthalpieen vast in het programma, de

constant

e

n

~orden

ingelezen via

FYSPRO.

De

gebruikte

referentie

temper

~

tuur

is 25 C,

(27)

( I

L

l _

r

i 1

I

l)

[1

II

n

Subroutine CONTR

calcul fase

ITESSPECM( 1 )

neen

0=0-40

24 -FIGUUR 25

ja

n e

Invoergegevens: SPECM(1)=n, n is de n

e

unit in d

r

rekenvolgorde

waarnaar

gesprongen wordt.

S?ECM(2)=t, t is de verlangde temperatuur.

(28)

r . I

1. r '

I

r'

_l₁

n

-

25 -[

FIGUUR

-261

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