U.S. patent number 3,617,493 [Application Number 05/002,258] was granted by the patent office on 1971-11-02 for process for steam cracking crude oil.
This patent grant is currently assigned to Esso Research and Engineering Company. Invention is credited to Charles E. Jahnig, Guy B. Wirth.
United States Patent |
3,617,493 |
Wirth , et al. |
November 2, 1971 |
PROCESS FOR STEAM CRACKING CRUDE OIL
Abstract
An improved process for steam cracking a crude oil feed to
produce products useful as chemical raw materials or fuels
characterized by the steps wherein the crude oil feed is first
passed through the convection section of a steam cracking furnace
to vaporize the materials in the feed boiling below about
450.degree. F., i.e., a naphtha fraction. The vaporized portion of
the crude oil feed is then separated from the liquid portion of the
feed by passing the liquid and vapor fractions into a separation
zone, i.e., a flash drum separator wherein the vaporized portion of
the feed passes overhead and is then fed, with steam, into the
steam cracking furnace and subjected to short residence time,
high-temperature cracking conditions. The liquid portion of the
feed i.e., nonvaporized portion which settles to the bottom of the
flash drum separator is withdrawn therefrom and passed through the
convection section of a second steam cracking furnace and
thereafter into a second separation zone. By introducing steam into
the second zone, i.e., flash drum separator, materials boiling
above about 450.degree. F. and below about 1,100.degree. F., i.e.,
the gas oil fraction of the crude, pass overhead from the separator
and are then introduced into a second steam cracking furnace,
without the need to further add substantial amounts of diluent
steam, to be cracked under optimum gas oil fraction cracking
conditions.
Inventors: |
Wirth; Guy B. (Florham Park,
NJ), Jahnig; Charles E. (Rumson, NJ) |
Assignee: |
Esso Research and Engineering
Company (N/A)
|
Family
ID: |
33161638 |
Appl.
No.: |
05/002,258 |
Filed: |
January 12, 1970 |
Current U.S.
Class: |
208/80; 208/92;
208/94; 208/130 |
Current CPC
Class: |
C10G
51/06 (20130101) |
Current International
Class: |
C10G
51/00 (20060101); C10G 51/06 (20060101); C10g
009/36 () |
Field of
Search: |
;208/80,92,100,94,130,132 ;260/683 |
References Cited
[Referenced By]
U.S. Patent Documents
|
|
|
3487006 |
December 1969 |
Newman et al. |
|
Primary Examiner: Levine; Herbert
Claims
What is claimed is:
1. A process for cracking a hydrocarbon feedstock which
comprises:
a. passing feedstock containing materials having boiling points
above and below 450.degree. F. into the convection section of a
steam cracking furnace to vaporize the materials in the feedstock
boiling below about 450.degree. F.;
b. introducing the vaporized and unvaporized fractions of the
feedstock into a first separation zone;
c. recovering the vaporized fraction of the feed from the first
separation zone and passing said vaporized fraction, with steam,
into the cracking zone of a first steam cracking furnace;
d. withdrawing the unvaporized fraction of the feedstock from the
first separation zone and passing said unvaporized fraction into
the convection section of a second steam cracking furnace, to
vaporize those materials boiling below about 1,100.degree. F.;
e. passing the vaporized and unvaporized fractions formed in step
(d) into a second separation zone;
f. introducing from about 0.1 to about 2.0 pounds of steam per
pound of hydrocarbon into said second separation zone; and
thereafter
g. recovering the vaporized fraction and steam from the second
separation zone and introducing said fraction containing steam into
the cracking zone of the second steam cracking furnace.
2. The process of claim 1 wherein from about 5 to about 50 vol.
percent of the materials in the feedstock have a boiling point
above 900.degree. F.
3. The process of claim 1 wherein the first cracking zone is
operated under cracking conditions which are optimum for cracking a
naphtha fraction.
4. The process of claim 1 wherein the second cracking zone is
operated under cracking conditions which are optimum for cracking a
gas oil fraction.
5. A process for cracking a hydrocarbon feedstock which
comprises:
a. passing a feedstock containing materials having boiling points
above and below 450.degree. F. into the convection section of a
steam cracking furnace to vaporize the materials in the feedstock
boiling below about 450.degree. F.;
b. introducing the vaporized and unvaporized fractions of the
feedstock into a first separation zone;
c. recovering the vaporized fraction of the feedstock from the
first separation zone and passing said vaporized fraction, with
steam, into the cracking zone of the first steam cracking
furnace;
d. withdrawing the unvaporized fraction of the feedstock from the
first separation zone and passing said unvaporized fraction, with
steam, into the convection section of a second steam cracking
furnace, to vaporize those materials boiling below 1,100.degree.
F.;
e. passing the vaporized and unvaporized fractions formed in step
(d) into a second separation zone;
f. recovering the vaporized fraction and steam passing overhead
from the second separation zone and introducing said fraction
containing steam into the cracking zone of the second steam
cracking furnace.
6. The process of claim 5 wherein from about 5 to about 50 vol.
percent of the materials in the feedstock of a boiling point above
900.degree. F.
7. The process of claim 5 wherein the first cracking zone is
operated under cracking conditions which are optimum for cracking
the naphtha fraction.
8. The process of claim 5 wherein the second steam cracking zone is
operated under cracking conditions which are optimum for cracking a
gas oil fraction.
9. The process of claim 5 wherein about 0.1 to about 2.0 pounds of
steam per pound of hydrocarbon is introduced into the second
separation zone.
10. A process for cracking a crude hydrocarbon feedstock which
comprises:
a. passing a feedstock wherein about 5 to about 50 percent of the
materials in said feedstock have a boiling point above 900.degree.
F. into the convection section of a first steam cracking furnace to
vaporize materials in the feedstock boiling below about 450.degree.
F.;
b. introducing the vaporized and unvaporized fractions of the feed
into a first separation zone;
c. recovering the vaporized fraction of the feed from the first
separation zone and passing said vaporized fraction, with from
about 0.4 to about 0.7 pounds of steam per pound of hydrocarbon,
into the cracking zone of the first steam cracking furnace;
d. withdrawing the unvaporized fraction of the feed from the first
separation zone and passing said unvaporized fraction into the
convection section of a second steam cracking furnace to vaporize
those materials boiling below about 1,100.degree. F.;
e. passing the vaporized and unvaporized fractions formed in step
(d) into a second separation zone;
f. introducing from about 0.2 to about 0.7 pounds of steam per
pound of hydrocarbon into said second separation zone;
g. recovering the vaporized fraction and steam passing overhead
from the second separation zone and introducing said fraction
containing steam into the cracking zone of the second steam
cracking furnace.
11. The process of claim 10 when the first separation zone is
operated at a pressure in the range of from about 30 to 100
p.s.i.g.
12. The process of claim 11 wherein the temperature in the
convection section of the first steam cracking furnace is in the
range of from about 450.degree.-750.degree. F.
13. The process of claim 12 wherein the vaporized feed is cracked
in the cracking zone of the first steam cracking furnace at a
temperature at the outlet of the furnace coil between about
1,500.degree. to about 1,700.degree. F. with a residence time in
the range of from about 0.1 to about 0.5 seconds and a steam
dilution of about 0.4 to about 0.7 pounds of steam per pound of
hydrocarbon feed.
14. The process of claim 13 wherein the convection section of the
second steam cracking furnace is at a temperature in the range of
from about 600.degree. to about 900.degree. F. fraction introduced
into the cracking zone of the second steam cracking furnace
comprises about 17 to about 38 wt. percent steam.
15. The process of claim 14 wherein the vaporized fraction
introduced into the cracking zone of the second steam cracking
furnace comprises about 17 to about 38 wt. percent steam.
16. The process of claim 15 wherein the vaporized fraction
containing steam which is introduced into the cracking zone of the
second steam cracking furnace is cracked at a temperature at the
outlet of the furnace coil at a temperature between about
1,350.degree. to 1,700.degree. F., said vaporized fraction having a
residence time in the cracking zone of from about 0.3 to about 0.6
second.
17. The process of claim 16 wherein about 50 vol. percent of the
materials in the feedstock have a boiling point above 900.degree.
F.
Description
FIELD OF THE INVENTION
This invention relates to an improved process for the steam
cracking of crude oil and heavy unsaturated hydrocarbon feedstocks.
More specifically, this invention relates to a two-stage process
for steam cracking a crude oil feed wherein about 50 volume percent
of the feed has a boiling point above 900.degree. F. In the
two-stage process of this invention, the feed is first passed to
the convection section of a steam cracking furnace to flash off
those volatile materials which vaporize below about 450.degree. F.
This vaporize portion of the feed, which corresponds approximately
to a naphtha fraction, along with the remaining liquid portion of
the crude feed is introduced into a separation zone, i.e. flash
drum separator. The vaporized portion of the feed passes overhead
from the separation zone and then being admixed with steam, is
introduced back into convection and then the radiant section of the
steam cracking furnace. The conditions under which the first
cracking furnace are operated are those conditions, i.e. residence
time and cracking temperature, which are optimum for the cracking
of a naphtha fraction to form valuable chemical raw materials. The
unvaporized, i.e. liquid portion of the feed is withdrawn from the
first separation zone and passed through the convection section of
a second steam cracking furnace and then introduced into a second
separation zone. Stripping steam is introduced either into the
liquid stream withdrawn from the first separation zone or into the
bottom portion of the second separation zone, i.e. flash drum
separator, to flash off i.e. overhead, materials boiling above
about 450.degree. F. and below about 1,100.degree. F., i.e. a gas
oil fraction. This vapor mixture, after leaving the second
separation zone, is cooled about 50.degree.-200.degree. F. in order
to liquefy a portion of said vapor mixture. Through this process,
entrained droplets of liquid hydrocarbon are washed from the vapor
mixture. Thereafter, the vapor fraction is introduced into the
convection section and then the radiant section of the second steam
cracking furnace. The cracking conditions employed in the second
steam cracking furnace are those which are optimum for the cracking
of a gas oil fraction. In this manner, both the naphtha fraction
and the gas oil fraction are each cracked under their own specific
optimum cracking conditions while eliminating the need for a crude
still to separately form a naphtha fraction and a gas oil fraction.
The cracking conditions (i.e. temperature, steam rate, pressure,
etc.) and severities can be selected to optimize the product yields
and minimize coking or operability problems for each feed stream.
In addition, the use of stripping steam in the second flash drum
separator serves not only to reduce the hydrocarbon partial
pressure in the flash drum and thus allow more hydrocarbon to
vaporize, but also provides the diluent steam, i.e. carrying and
cracking medium, for the vaporized hydrocarbon fraction passing
overhead from the second separation zone into the second steam
cracking furnace. The products formed in the cracking process may
then be separated using well-known separation techniques.
DESCRIPTION OF THE PRIOR ART
Conventional steam cracking processes are generally well known in
the art and have been widely used in the preparation of valuable
unsaturated hydrocarbon compounds and olefins by the thermal
cracking of various hydrocarbons or hydrocarbon feedstocks.
Nevertheless, crude oil has not been employed as a hydrocarbon feed
in the steam cracking processes owing to the high degree of coking
that results in the tubes in the furnace. Consequently, in
conventional processes for the conversion of crude petroleum into
more valuable hydrocarbon products, a combination of crude oil
distillation and conversion processes have been employed.
Typically, the crude oil is fractionated in a crude still into a
light fraction, i.e. naphtha, a middle fraction, i.e. gas oil and a
heavy residuum fraction, i.e. topped crude. Either the naphtha or
the gas oil fraction can be subsequently subjected to
thermal-cracking, i.e. steam cracking or catalytic refining
treatment processes to obtain lower boiling products, i.e.
ethylene, propylene, butadiene and the like. The topped crude is
generally subjected to a further distillation at reduced pressure
in a vacuum still to recover a light fraction, i.e. vacuum gas oil
and a heavy fraction, i.e. vacuum residuum. The vacuum gas oil may
then be steam cracked or catalytically treated, as above, and the
vacuum residuum is burned as a fuel or upgraded by conversion
processes such as coking.
For economical heat recovery, much heat exchange apparatus is
required both within each unit and in combination between units.
The vacuum distillation equipment normally employed for
fractionating the reduced crude is expensive with respect to
investment, operation and maintenance.
In addition, optimum conditions for steam cracking the above
feedstocks, i.e. naphtha and gas oil, are different for each feed.
For example, naphtha feeds require a higher temperature in the
cracking zone than a gas oil. These temperatures are imposed
largely by fouling or coking of the cracking coil as well as by the
kinetics of the cracking reactions.
Furthermore, the type of crude oil which is employed as the
hydrocarbon feed significantly affects the percentage of the
naphtha and gas oil fractions obtained and thus the amount of the
crude which can be ultimately subjected to thermal cracking
processes. For example, in Netherlands Pat. application Ser. No.
6,814,184, a process is described wherein a crude oil feed, having
a high gasoline content is heated with steam in the convection
section of a cracking oven; passed into a separation zone where
nonvolatilized components are separated off, and thereafter the
volatilized components are thermally cracked. A major deficiency
associated with such a process is that lower temperatures must be
used in the cracking zone to prevent fouling. This results in
significant losses in yields to valuable low molecular weight
hydrocarbons than could be realized when the naphtha and gas oil
fractions are cracked separately. Another deficiency associated
with this process is that with only one separation zone, crudes,
particularly heavy crudes, i.e. crudes with high average boiling
points, are not vaporized as completely as can be accomplished in a
crude still. Thus, some of the valuable gas oil is not vaporized
and is burned as fuel. From a practical standpoint it is essential
to avoid entrainment of residual liquid in the flash zone since it
would excessively foul the convection or radiant section of the
furnace. Therefore, special precautions must be taken, as described
above. Thus, the art is in need of an economic process for the
thermal cracking of crude oils, particularly heavy crude oils
wherein about 50 volume percent of the crude oil has a boiling
point above 900.degree. F. under such conditions that maximum
yields are obtained from the more valuable naphtha and gas oil
fractions.
SUMMARY OF THE INVENTION
It has now been discovered that the heretofore mentioned attendant
difficulties in the cracking of crude oil may be overcome by
employing the two-stage flash process of the instant invention. In
accordance with the instant invention, the crude oil feed is passed
into the convection section of a steam cracking furnace wherein the
temperatures are in the range of from about 450.degree. to
700.degree. F. in order to vaporize the materials in the feed
boiling below about 450.degree. F. the vaporized portion of the
crude feed, which is in the range of from about 20 to 50 wt.
percent based on feed, is then introduced along with the liquid
portion of the feed, i.e. that portion of the feed which was not
flashed in the convection section of the furnace, into a separation
zone, i.e. a flash drum separator. The separation zone is operated
at a pressure of from about 30 to about 100 p.s.i.g. or greater
such that the vaporized portion of the feed passes overhead and is
then admixed with about 0.1 to 2.0, and more preferably 0.4 to 0.7
pounds of steam per pound of hydrocarbon before being introduced
into the cracking zone in the steam cracking furnace. Thus, the
feed to the first cracking zone comprises about 10 to 67 wt.
percent steam in order to lower the hydrocarbon partial pressure
and thus increase yields to low molecular weight hydrocarbons. This
vaporized portion of the feed, which approximates a naphtha
fraction, along with the above-described amount of steam, is
cracked in the radiant section of a steam cracking furnace under
those conditions which are optimum for the cracking of a naphtha
fraction. Thus, the vaporized feed in the cracking zone is cracked
at a temperate at the outlet of the furnace coil between about
1,500.degree. to about 1,700.degree. F., with a residence time in
the radiant section, i.e. cracking section of the steam cracking
furnace of about 0.1 to 0.5 seconds with a steam dilution of about
0.4 to about 0.7 pounds of steam per pound of hydrocarbon feed.
The liquid portion of the crude feed which forms a liquid phase in
the bottom portion of the first flash drum separator is withdrawn
therefrom and passed through the convection section of a second
cracking furnace wherein the feed is heated to a temperature of
from about 600.degree. to about 900.degree. F. Since low boiling
materials have been removed in the first flash zone, it is now
possible to operate this second convection zone at a higher
liquid/vapor ratio, which improves heat transfer and reduces the
fouling tendency. The materials which are vaporized by being passed
through the convection section of the second cracking furnace are
those materials in the crude feed which vaporize below about
850.degree. to 1,100.degree. F., more preferably about 950.degree.
F. These vaporized materials comprise about 35 to 90 wt. percent of
the unvaporized material withdrawn from the first flash drum and
about 15 to 25 wt. percent based on total crude feed. This
vaporized portion of the feed along with those materials which have
not been vaporized by passage through the convection section of the
second cracking furnace, are passed together into a second
separation zone. Steam is introduced into the hydrocarbon stream
before entering the convection section of the second cracking
furnace or into the second flash drum or into both in order to
strip the gas oil fractions from the heavy residua and to provide
diluent steam for the subsequent steam cracking process step. This
steam can be preheated above the oil temperature to provide
additional heat. The amount of stripping steam which is employed is
in the range of from about 0.1 to 2.0, and more preferably from
about 0.2 to about 0.7 pounds/steam per pound of hydrocarbon feed
such that the feed to the second cracking zone comprises about 17
to 38 wt. percent steam. The gas oil fraction along with steam,
thus passes overhead from the second separation zone and is passed
into the second cracking zone in the radiant section of the second
steam cracking furnace. The conditions in the second cracking zone
are those optimum conditions for steam cracking a gas oil fraction.
Accordingly, the contact time of vaporized portion in the second
cracking zone, i.e. radiant section of second steam cracking
furnace is in the range of from about 0.1 to 1.0 seconds,
preferably 0.3 to 0.6 seconds. The temperature at the coil outlet
of the cracking zone i.e. the radiant section of the furnace, is
within the range of 1,350-1,700.degree. F. Pressures within the
tubes may range from 10 to 200 p.s.i.g. at the coil outlet. The
liquid portion remaining in the bottom of the second flash drum,
i.e. heavy residua of the crude feed oil, may be stripped with
steam and withdrawn and employed as a fuel. Thus, it can be seen
that the two-stage flashing process of the instant invention
provides both an economical and technical advance over the prior
art.
Economically, the present invention eliminates much of the heat
exchange apparatus which was heretofore required, while utilizing
the convection sections of the cracking furnace to vaporize those
fractions, i.e. naphtha and gas oil fractions which may be
conventionally steam cracked to produce high yields of valuable
chemical raw materials. In addition, a significant advantage of the
instant process is the steam cracking of crude oils and hydrocarbon
feeds wherein about 50 volume percent or higher of the materials in
said feed have a boiling point above 900.degree. F. Furthermore,
the use of the two-stage process of this invention allows the
naphtha fraction and the gas oil fraction each be cracked under
their optimum cracking conditions in order to increase overall
yields of unsaturated cracked hydrocarbon products, especially
C.sub.4 --C.sub.6 diolefins such as butadiene, isoprene and
cyclopentadiene and the like without significant loss of ethylene,
etc. Moreover, special equipment such as a heat exchanger on the
furnace effluent (to make steam) can then be used on the naphtha
cracker, whereas it is not considered operable with gas oil
feeds.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
Having set forth its general nature and advantages, the invention
will be best understood from the more detailed description
hereinafter which refers to the accompanying drawing, wherein a
schematic flow diagram of the steps used in the present invention
is shown.
Referring to the drawing, a crude oil feed is fed by way of line 1
through the convection section of a cracking furnace 2 in order to
flash off i.e. vaporize that portion of the feed which boils below
about 450.degree. F. It is to be understood that other feeds in
addition to crude oils may also be employed in the practice of the
instant invention. Other feeds include, but are not limited to,
hydrocarbon feedstocks wherein about 5 to about 50 volume percent
of the materials in such a feedstock have a boiling point above
900.degree. F. As mentioned above, a significant advantage of the
instant invention is that feedstocks wherein as high as about 50
volume percent of the materials in such feedstock have a boiling
point above 900.degree. F., may be successfully employed in the
process of this invention.
The vaporized portion of the crude feed along with the nonvaporized
portion are passed by way of line 3 into the upper portion of a
flash drum separator 4. The flash drum separator 4 is operated
under a pressure in the range of from about 30 to about 100
p.s.i.g. in order to effect a phase separation between the gas
phase containing approximately the naphtha fraction and the liquid
phase containing that portion of the feed which comprises above
about 30 wt. percent based on total feed. The vaporized portion of
the feed thus passes overhead by way of line 5, is admixed with
steam via line 6 and reintroduced back into the convection section
of the cracking furnace via line 7. The conditions under which the
cracking furnace is operated are those which are optimum for the
cracking of a naphtha fraction, as described above. These cracking
conditions increase the cracking selectivity to C.sub.4 --C.sub.6
diolefins such as butadiene and isoprene over that which would be
obtained by cracking the naphtha and gas oil fractions together at
other than optimum conditions for the naphtha fraction.
The unvaporized, liquid portion of the feed which settles to the
bottom of the first flash drum separator 8 is withdrawn therefrom
and passed by way of line 9 through the convection section of a
second cracking furnace 10. The temperature of the liquid which is
withdrawn from the flash drum separator is in the range of about
450.degree. to about 700.degree. F. After passing through the
convection section of the second cracking furnace, the temperature
of the feed has been raised to about 600.degree. to about
900.degree. F. The portion of the feed which has been vaporized by
passing through the second convection zone 10 along with the
remaining liquid portion of the feed is passed by way of line 11
into a second flash drum separator 12. The second flash drum
separator is operated at a pressure in the range from about 30 to
about 100 p.s.i.g. Steam is introduced into the second flash drum
separator 12 by way of line 13 or into line 9 in order to reduce
the partial pressure of the hydrocarbon in the flash drum in order
to increase the vaporization of the hydrocarbon and to provide
diluent steam for the subsequent steam cracking of the vaporized
products recovered from the second flash drum separator. The
vaporized products, which are produced by passing the feed through
the convection section of the second cracking zone and by steam
stripping, are passed overhead from the flash drum by way of line
14 into the convection section of the second cracking furnace and
thence through the radiant section from which the cracked products
are recovered. The vapor leaving the separator is cooled about
20.degree.-200.degree. F. to condense a small part of the vapor
stream in a partial condenser 15. The condensed portion is used to
scrub or wash the vapor stream to remove droplets or mist particles
that are carried by the vapor stream. Removal of the droplets are
necessary to prevent fouling of the steam cracker coil by heavy
fractions contained in said droplets. The residue from the second
flash drum separator, which is in liquid phase, is withdrawn from
the flash drum separator 12 by way of line 14.
* * * * *