Hydrogen Production from Partial Oxidation of Residual Fuel Oil

6 Hydrogen Production from Partial Oxidation of Residual Fuel Oil

Downloaded by UNIV OF SYDNEY on October 5, 2015 | http://pubs.acs.org Publication Date: March 26, 1980 | doi: 10.1021/bk-1980-0116.ch006

C. L. REED and C. J. KUHRE Process Engineering-Refining Department, Shell Oil Company, 1100 Milam Building, P.O. Box 3105, Houston, TX 77001

In the past several years, forecasting the future avail-

ability and prices of hydrocarbon feedstocks for hydrogen

manufacture has been a very difficult problem. Today, in addition to the supply and demand forces of the market place,

the indeterminate influence of future governmental regulations greatly magnifies the dilemma faced by a company trying to select a long-term economical feedstock for a new hydrogen plant. For many years steam reforming of natural gas to pro-

duce synthesis gas has been a favored basis for hydrogen plant operation. However, the potential for increased price of natural gas has now directed attention to selection of heavier hydrocarbons as feedstock for hydrogen plants. A process which is well-suited to the basic requirement of providing hydrogen and carbon monoxide for hydrogen

manufacture is the partial oxidation of hydrocarbons; i.e.,

the combustion of hydrocarbons with a limited amount of oxygen to yield hydrogen and carbon monoxide. The process is also referred to as gasification because it converts liquid hydro-

carbons to gaseous products, essentially H2 and CO with only small amounts of CO2 and CH4 when high-purity oxygen is used as the oxidant. The product gas, often called synthesis gas or "syngas", can then be converted to high-purity hydrogen as well as a great variety of other chemical products. The ratio of hydrogen to carbon monoxide in the synthesis gas product from the partial oxidation unit is mainly a function of the hydrogen and carbon content of the feedstock. However, it is possible to exchange over a CO-shift catalyst the carbon monoxide of the synthesis gas for hydrogen from steam while simultaneously producing carbon dioxide. The processing sequence chosen for this paper, shown in Figure 1, is a conventional hydrogen plant flow scheme with each process section having been commercially well-proven. The synthesis gas product from the Shell Gasification Process

(SGP) unit is treated for sulfur removal in a Shell Sulfinol

unit.

The CO-Shift unit includes high-temperature shift cata0-8412-0522-1/80/47-116-095$06.75 © 1980 American Chemical Society In Hydrogen: Production and Marketing; Smith, W., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1980.

96

HYDROGEN: PRODUCTION AND MARKETING

!

>

i

!

cc cc u. >

j

>

i

=8

i

5s

J

co lu

¦

;

?....„¦

8+

-âMs

T

ft

I

^

|5

I

CN

2 N

-5

Ü w

ii

,P i

1

.gS? S

CN

g

$

i—

CT» s

§S°°° V n/

£ z:

U CU u

Q.

~.

^ S ri—

LO s

_^ =3 CU

u. uj _ i h-

m -a

COVO-"-*o:^.o.^.o°.

=3 -

it-

£

^^ i^g

CO CO

U £

> Q.

ä

^co

•— .

TO

r= £ =3 ^5

r-

s':^ g "O O CD

•

O

S-

i3 oo CU -r-

h ,~

ct. .r^ -co

kDOOCOOOOO

^

^

£

CU CU u ^; o to £r

n'r~ C CU

£ a; CQl =3

•

h: ^T .=3

T-^?4" ^ 'ü c n ,* _c

i. "T*

^^;;

00 c

•—

C3_Oi_QJCU

_ia

^ °

«a O

coh--o-ocj=3°°

-3^3^:^: go + CO CO

S

=3

QJ

4->

5 .

^

t-

3

s.

~^

CNJ CO •

O

-O

>>

*+-

s-

JC

r~"

*— • OO

Q_ X CD

l_J

_J .,_.,-

4-> .r-

_J

>

__

O

CD

C

C

Cr-CCn

=C ZD T3

C* *tf- CM CM r-

LOO OOOO

^_DCJ4->OQ-

d Q. rL--

«_ o

CL. Ll.

--

to"

i S

oo 5

O

CG

CT.

VO

C* Kt

LO

vo

ZI

H-O-3C0

"O "D o o

CO «i—

4->3Z3C0 -r«^

.

Si- .2o»§< •— « O z c.

r— • O O

«4_.p-.r-r—

H-LxjM-r~.

C"

r~~

Q-

03-OX

ZD

CM 5

O

"r-.o 03 0

CDCDCD CD -C T3 M4-> CD CD to CO

VO 00 O »ri—

CGOOr— _C CC _- O 4->

to

I

•»CD

O

«i—

+ c

CDCD

c en c c c en

0000'>

>

O0IJCSO o

^ ^ Pc O CD O

To 5 x > £ § ^c_§o

M-

EEEC

_c -5 ^T

-ü ^

.?

r-

u

o.

O

CO

"^

00

CD

CD^H-CO

•r- s^ _q jd. x: s4-> "O S- S- 4-> 4-> •r- >) «O fO Ol -r-

eu E 4->l fO-Û

glOO^Z

«--

s$_ $^^-^S £ £ £ g* ^

£L

^

2*

en

03

en

p

s-

^

^O o

* CD s-

ti ^ _^

7) OJ +f

ti _> _=£

P ¦*= ..

r-

3

"g

g

-g

«

In Hydrogen: Production and Marketing; Smith, W., et al.; ACS Symposium Series; American Chemical Society: Washington, DC, 1980.

6. reed and KUHRE

Partial Oxidation of Fuel Oil

101

TABLE III, SGP BASED HYDROGEN PLANT


ESTIMATED CAPITAL INVESTMENT

Basis: Feedstock Production toofthe100 SGPX 106is heavy scf/stream day H2. fuel oil Estimated Installed

Plant Section

Capital Cost,a)$106

Gasification

27.0

Sulfinol

5.4

C0-Shift

14.0

Auxiliary Oil -Fi red Boiler

7.2

C02-Removal & Methanation

9.4

Offsites (35%)b) Total

22.0 85.0

a)ßasis: mid-1979, U.S. Gulf Coast, installed costs. No allowance made for interest during construction.

^/Offsites estimated at 35% of onsite capit. 1 to cover such items as

cooling water, feed water preparation, "tilities, feedstock storage,

effluent treating, and other minor offsites required for a plant

installed adjacent to an existing facility. Oxygen is considered to be delivered "over the fence" at the required pressure and no capital

allowances are included for this supply.


102


oo o c\ i— 3= S- M-_ CD CJ

*dCjT> •

r— O •

VO OO •

OO •— •

i— VO i— OOLO • * *


ÛL.00OOOOOO«—

00

CD«—

o vo

OO i—

>-

S~

CMOïCNJCMOïl^

•••••••

i— 00

Oi — f—

^

O

i—

VT> ^

CD •feO- Cv_ CNJ H-

2:

i«TJ CD

OO

m

oo

>> en s-

H-

>>

> LU

•— «

CD OO

03

% >

CD O

H
«TJ -C +->

r— -Q

CD CD

Q_ «3

jc

03

03 > i> X

S-

03 O

•!S4->

en

o3 oo

03

U_

2:

O

CD

»r-

S-

CL

Û_

Û.

-r-

CD

CD

03

CD

CD

O

O

-C

i—

>

O0

OO

00

CÛ

CJ

LU

•r-

.—

E

CD

s

00

00 4->

o CJ

i—

'O 4-> O H-

O


6. reed and KUHRE

Partial Oxidation of Fuel Oil

i cd r^

103

•

-o *a- >> oo i— CO Q. O M- O•r- O Z3

E O0«^-LOLO"^-| — O «— O o «dr.

.

.

•

.

•

CM CM .


OOOOOOCM

VOCMOOLOOOr—

CO

LO

1^

1^

*d"

CM

O

.......

O^d-i—

f—

^d-O0O0 i— cm r^

-M So Q.

to

Q.

C0OC OCDCD

00

O

00

U U

CD

CD X >> CD

X O

13 *>

C

I— 03 C c -r- «+_ o o

O '•00 .,>

•r- CD -u> +j >>

SCD

•r"O "O

03 +-> S- -iCD i—

Q. Z3 tO

O JÛ

-P

03Q.T-

S-030 O >>•«CD

«4- r- ri— CD

ST-

LO 03 SE cd s- c i— O O

"O * ^

_Q 03 H-

4-> M«r-

C

CL =3

CO

+-> en

CD »r-

C

x: c -r4-> 3 -o

00 4-> +->

cd ••- s: cls:

2: 2:

* 03 ^

\

QJ

00 «i- "O

Û.W UO 4-> ^

E "O U C C (O •r- ro f-

*>903 •

t- O) c cn CT> CTl +J D)'r S S S 03c c* cr> cr> S- m- i— r— i— i—

O Sto+J»EEE UT3+J VO 03 CDOO S- 4- $- S- SECC 4-> O O O O 13 -r- O • S- X M- M- M«i-03t0OCD^ 00 +-> fc^ +-> JQ r^"0"0"0 O C LO 00 03 1— 1 — CDCDCD Q-T-a» Oi— 1— EEE E03/NO OtH-I3=5Z3 >> E 4-> S- O 00 C0 00 OO CT> O >> C0 00 00 1— S-r»-CD03CD030303 >>«— 03 œ> s- a. en .QCDCD«— *«-$->>>>>> 2 >> I -0"D 00(JjQC:jQ-Q_Q Q.030303C03CS-S-S00+J-OCÛMr-
CD CDCJ O X CJ h-rC i— LU 03 03 S4-> r— 13 -r03 tO CL +J»

«£

CD 03 4-> CnjQ 4-> C 00

-C Û_ E o cd «3

00 4_> 00 O CJ

S

•

O0

O QJr-V> '"-J C 1—

00 +j 00

•I-Q-03-OC03

03

O O

•

-Q M- CD CM

• 3 SC OO O 03 4~>

00 4_> 00 O CJ

Z3 4-J

cû

CD

Mr— ^

sO _Q 03 I

• 3 • i — 4->

x: u 03 oq s-

------- 1- -O

^¦^ CJ

• > nz CD

C

CD r— CD CD O Q. 00 C

• > m CD

I

OO

CD

CD S- 03 I I I cm- +j*a -OTJ O

I

O *r- -r- -I-

O

^^

^-^^^

^-^^-s^-^^-^

H-

TJ

i3 U

"O QJ^H CD


104



So JD 03 i—

S-

i03

—

f—

CT>

00 00 03

r-* CT> r— I

CD

TD

•1-

"""

>>

4->

•«4->

iCD >>

>> 03 "D

en C

I

03

03

CD

Cl

CD

\

O

Q_

E

00

CM

cn

\

S-

03

S-

00 O 4_ OOM_ * O

^-^ r—

OOLOOO

O

S^

OO^t-O

CO

fcS.

LO

frS.

O0

r—

OOCMOO

V>

1—

LO

•r-OOOO _»I

c •«-

C

00 03

03 CD

CD

>>

sO _Q 03

....

r—

13 4-> CO.

00 00

VO

?
CD

r-

LU O _J »-H

^—» ZJ

CÛZ CD

VO

O LU

O r— ^

~ 0_ ^-^ 1— 03

o t-

CD

cn

O 4-> CJ

1— 03 4->

C «i4->

03

-r-

03

en

^ _c_

00

iCD 1— •«O CQ

£>

O 4->

03 tf— -rX 3

"O cd

S-

O OO 4_) 00 O

-bO-

Hydrogen Production from Partial Oxidation of Residual Fuel Oil

Recommend Documents