U.S. patent number 3,869,378 [Application Number 05/173,699] was granted by the patent office on 1975-03-04 for combination cracking process.
This patent grant is currently assigned to Sun Oil Company of Pennsylvania. Invention is credited to James M. Durrett, Andre W. Pollock.
United States Patent |
3,869,378 |
Pollock , et al. |
March 4, 1975 |
**Please see images for:
( Certificate of Correction ) ** |
Combination cracking process
Abstract
This invention relates to a process for combined catalytic
cracking and catalytic hydrocracking comprising a hydrocracker, a
low severity catalytic cracker operating at a reactor temperature
of at least about 900.degree. F., and a high severity catalytic
cracker operating at a severity essentially greater than said low
severity catalytic cracker. A heavy virgin petroleum feedstock
boiling from at least about 700.degree. F. to at least about
1,000.degree. F. is cracked in the low severity cracking zone and a
light virgin petroleum feedstock boiling from at least about
400.degree. F. to at least about 700.degree. F. is cracked in the
high severity catalytic cracking zone. The combined catalytic gas
oils produced from the two catalytic crackers are processed in the
hydrocracking zone and the heavy product from the hydrocracker is
recycled to the high severity catalytic cracking zone.
Inventors: |
Pollock; Andre W. (West
Chester, PA), Durrett; James M. (West Chester, PA) |
Assignee: |
Sun Oil Company of Pennsylvania
(Philadelphia, PA)
|
Family
ID: |
22633129 |
Appl.
No.: |
05/173,699 |
Filed: |
November 16, 1971 |
Current U.S.
Class: |
208/78; 208/56;
208/80; 208/68 |
Current CPC
Class: |
C10G
11/18 (20130101); C10G 11/00 (20130101); C10G
47/00 (20130101) |
Current International
Class: |
B01j 009/20 ();
C10g 037/02 () |
Field of
Search: |
;208/78,68,80,56 |
References Cited
[Referenced By]
U.S. Patent Documents
Other References
Arey & Kronenberger, "Hydrotreat Cat-Cracker Feedstocks," Oil
and Gas Journal, May 19, 1969, pp. 131-139..
|
Primary Examiner: Coughlan, Jr.; Paul M.
Assistant Examiner: Schmitkons; G. E.
Attorney, Agent or Firm: Church; Mr. George L. Johnson; Mr.
Donald R. Dixon; Mr. Anthony J.
Claims
We claim as our invention:
1. A process for treating petroleum which comprises
a. catalytically cracking, in a first cracking zone, a heavy virgin
feedstock at a temperature of at least about 900.degree. F.,
b. catalytically cracking, in a second cracking zone, a light
virgin feedstock at a severity essentially higher than that in step
a,
c. separating in a distillation zone an aromatic cycle oil from the
cracked products of steps a and b,
d. catalytically hydrocracking the aromatic cycle oil produced in
step c in a hydrocracking zone,
e. separating the bottom fraction boiling above at least about
400.degree. F. from the effluent of step d in a distillation zone,
said bottom fraction, being of sufficient paraffin content, that is
at least about 70 percent due to the catalytic hydrocracking of
step d to comprise an acceptable catalytic cracker feedstock
without further processing and
f. recycling said bottom fraction produced in step e to the
catalytic cracking zone of step b.
2. The process of claim 1 wherein the bottom fraction from the
distillation zone of step e is recycled to the catalytic cracking
zone of step a.
Description
DESCRIPTION OF THE PRIOR ART
In the prior art, crude petroleum has been separated into fractions
of different boiling range and the separate fractions treated
individually by thermal, catalytic, hydrogenative, and
hydrocatalytic processes. In each of these processes it is
characteristically observed that a portion of the feed is converted
to desired products leaving material which, when recycled, is less
readily converted than the feed. For example, in catalytic cracking
of gas oils, a part of the feed is converted to the desired
gasoline and lighter products, a part is converted to coke, which
provides most of the heat needed in the process, and the remainder
is converted to light and heavy cycle oils which are considerably
more refractory when recycled back to the cracking unit, i.e., more
difficult to crack than the feed. The excess cycle oils produced
are generally disposed of in heavy fuel oil. Likewise, in catalytic
hydrocracking processes it is observed that a portion of the feed
is readily hydrocracked to lower boiling distillates, leaving
another portion, mainly paraffinic, which is more resistant to
further hydrocracking.
It is therefore a primary object of this invention to combine
hydrocracking and catalytic cracking processes in such a way as to
use each process for the type of feed it is better suited to
convert to the more desirable gasoline and lighter products.
Hydrocracking is far superior to catalytic cracking in bringing
polynuclear aromatic components down into the gasoline range.
Catalytic cracking, on the other hand, can achieve higher
conversions when operating at higher severity on paraffinic and
naphthenic stocks. The highly aromatic cycle oils produced in the
catalytic cracking process are an excellent feedstock for the
hydrocracking process and the unconverted paraffinic portion of the
hydrocracker feedstock is a suitable feed for a highseverity
catalytic cracking operation.
The most pertinent prior art is U.S. Pat. No. 3,193,488 issued to
Donald E. Carr of Phillips Petroleum Company, July 6, 1965. This
patent discloses catalytically cracking, in separate zones, a
topped crude and a gas oil, solvent extracting the aromatic extract
from the resulting cycle oils, which is subsequently hydrocracked,
leaving a paraffinic raffinate, which is recycled to the gas oil
cracker. A heavy product from the hydrocracker is also solvent
extracted to produce an aromatic recycle to the hydrocracker and a
paraffinic recycle to the gas oil catalytic cracker.
SUMMARY OF THE INVENTION
If the respective catalytic cracking zones and the hydrocracking
zone are operated at sufficient severity, the intermediate
extraction zones can be deleted. Said severity levels are defined
herein as a reactor temperature of at least about 900.degree. F. in
the low severity catalytic cracker, and a severity in the second
catalytic cracking zone essentially above that in the low severity
cracking zone. This higher severity can be obtained through
increasing reactor temperature, increasing catalyst to oil ratio
and other methods. The proper combination of conditions for a given
operation can be readily determined through experimentation by one
skilled in the catalytic cracking art.
A second object of this invention is to provide a process for the
simultaneous conversion of two different virgin feedstocks in
separate catalytic cracking zones under particular conditions
suited to each feed whereby the maximum yield of lighter more
valuable products is obtained.
These objects and other advantages of the invention will become
apparent from the description of the process. By a light virgin
feedstock, as the term is used in the description, is meant a
distillation fraction obtained from natural crude oil, said
fraction boiling mainly in the range from 400.degree. to
700.degree. F., and the use of the term heavy virgin feedstock is
intended to mean that portion of natural crude oil which boils
mainly in the range from 700.degree. to 1,000.degree. F. Recycle
stocks and recycle oils are defined as cracked petroleum fractions
boiling above gasoline. Low severity catalytic cracking is defined
as a cracking operation of at least about 900.degree. F., and high
severity catalytic cracking is defined as a cracking operation at a
severity essentially above the low severity temperature.
DESCRIPTION OF THE DRAWING
The invention is best explained by referring to FIG. 1.
A light virgin feedstock introduced from an outside source via
conduit 1, is charged to the high severity fluid catalytic cracking
zone, 2. The effluent from cracking zone 2 is withdrawn through
conduit 3 and charged to the distillation zone, 4, where it is
fractionated into at least an overhead product and a catalytic gas
oil. The overhead product is withdrawn via conduit 5 for further
processing in an outside unit and the catalytic gas oil is
withdrawn through conduit 6 and charged through conduit 7 to the
hydrocracking zone, 8. The effluent from the hydrocracking zone 8
is withdrawn through conduit 9 and routed to the distillation zone
10 where it is separated into at least an overhead product and a
bottoms product. The overhead is withdrawn via conduit 11 and sent
to an outside unit for further processing. The bottoms product is
withdrawn via conduit 12 and recycled to the high severity
catalytic cracker 2, via conduits 12 and 1.
A heavy virgin feedstock, introduced from an outside source via
conduit 13, is charged to the low severity fluid catalytic cracking
zone, 14. The effluent from cracking zone 14 is withdrawn through
conduit 15 and charged to the distillation zone, 16, where it is
fractionated into at least an overhead product, a middle-boiling
product and a heavy product. The overhead product is withdrawn via
conduit 17 for further processing in an outside unit, and the
mid-boiling catalytic gas oil is withdrawn through conduit 18 and
charged through conduit 7 to the hydrocracking zone 8. The effluent
from the hydrocracking zone 8 is withdrawn through conduit 9 and
routed to the distillation zone 10 where it is separated into at
least an overhead product and a bottoms product. The overhead is
withdrawn via conduit 11 and sent to an outside unit for further
processing. The bottoms product is withdrawn via conduit 12 and
recycled to the high severity catalytic cracker, 2, via conduits 12
and 1.
The heavy, high-boiling product from distillation zone 16 is
withdrawn via conduit 19 and recycled to the low severity catalytic
cracker via conduits 19 and 13.
DESCRIPTION OF THE PREFERRED EMBODIMENT
By operating the catalytic cracking zones and the hydrocracking
zone at sufficient severity, each can supply a suitable feed for
the other without the necessity of intermediate processing of said
feed streams. An illustrative example shows the benefits that may
be gained by practice of this invention.
Referring to Table 1, two catalytic cracking operations are shown,
one at 950.degree. F. reactor temperature and one at 1,000.degree.
F. reactor temperature.
TABLE I
__________________________________________________________________________
Case 1 2
__________________________________________________________________________
Fresh Feed 30.8.degree.API Fresh 30.8.degree.API Fresh Gas Oil Gas
Oil Fresh Feed Rate, 60,000 60,000 B/D Reactor Temperature,
.degree.F. 950 1000 Catalyst/Oil Ratio W/W.sup.(1) 7.4 9.0 Reactor
Pressure, psig 21.0 21.0 Recycle Rate, B/D 0 0 Conversion, Vol.
Percent 71.64 80.11 Fresh Feed Yields, Percent Fresh Feed: C.sub.2
and lighter, Vol. Percent 4.68 6.00 C.sub.3 's, Vol. Percent 12.48
16.08 C.sub.4 's, Vol. Percent 18.10 23.33 C.sub.5 + Gasoline, Vol.
Percent.sup.(2) 47.34 47.66 Light Cycle Oil, Vol. Percent 17.36
13.89 Heavy Cycle Oil, Vol. Percent 10.00 5.00 Clarified Oil, Vol.
Percent 1.00 1.00 Gasoline F-1 O.N. Clear 92.9 94.6 Heavy Cycle Oil
Properties: Gravity, API at 60.degree.F. 19.4 9.0 Initial B.P. TBP
.degree.F. 580 583 20% Pt., do. 598 596 80% Pt., do. 690 675 Final
B.P. do. 766 708 C.sub.A, %W.sup.(3) 44.8 64.9 C.sub.N, do..sup.(3)
11.3 7.4 C.sub.P, do..sup.(3) 43.9 27.7
__________________________________________________________________________
.sup.(1) lb. catalyst/unit time divided by lb. oil/unit time.
.sup.(2) conversion basis, 375.degree.F. at 90% point gasoline.
.sup.(3) weight percent carbon atoms in aromatic, naphthenic, and
paraffinic structures, respectively.
As can readily be seen, the heavy cycle oil from Case 2 which would
constitute the feed to the hydrocracking zone, is of sufficient
aromaticity to be processed in said hydrocracking zone without
intermediate processing. Further advantages can be seen in the high
severity level which can be reached in the catalytic cracker which
will handle the lighter feedstock, resulting in higher conversion
levels and extremely high aromatic content in the heavy cycle oil
produced therein.
The data on Table 2 represent a hydrocracking operation on heavy
catalytic cycle oil of the type produced by the catalytic cracking
phase of the novel combination process being described herein. The
400.degree. F..sup.+ bottoms product withdrawn from the
hydrocracking zone constitutes an additional feedstream to the high
severity catalytic cracker previously discussed.
TABLE II ______________________________________ Reaction
Conditions: Hydrocracker Temp., .degree.F. 726.degree.F. Pressure,
psig 1550 LHSV, V/Hr./V 0.87 H.sub.2 Consumption, SCF/Bbl. feed
2501 400 .sup.+.degree.F. Product, Vol.% Fresh Feed 79.5 650
.sup.+.degree.F. Product, Vol.% Fresh Feed 20.5 Properties,
450-650.degree.F. Cut: Gravity, API at 60.degree.F. 25.9 Nitrogen,
PPM 1 Sulfur, PPM 15 ______________________________________
If the heavy catalytic cycle oil is recycled directly to the high
severity catalytic cracker, the product slate which results
reflects the refractory nature of this stream, that is the
difficulty with which it cracks. However, if the 400.degree.
F..sup.+ hydrocrackate of this heavy cycle oil is recycled, to the
high severity catalytic cracker, as is disclosed herein, the
increase in conversion at identical conditions shows the
improvement of this stock as a catalytic cracker feed. Such a
comparison is shown in Table 3.
TABLE III ______________________________________ Case Base Case 1
______________________________________ Chargestock Heavy
400.degree.F..sup.+ Catalytic Hydrocrackate Cycle Oil Bottoms
Operating Conditions: Reactor Temp. .degree.F. 1010 1010 Catalyst
to Oil 6.0 6.0 Ratio, W/W Pressure, psig 20 20 Conversion, Vol.%
28.3 60.2 Fresh Feed.sup.(1) Product Yields: C.sub.2 and lighter,
Vol.% 3.2 3.9 C.sub.3 's , do. 5.5 11.7 C.sub.4 's , do. 6.5 15.4
C.sub.5 + Gasoline , do. 13.0 40.0 Coke , Wt.% 7.0 3.3
______________________________________ .sup.(1) 375.degree.F. at
90% basis
As seen in Table 3, 400.degree. F..sup.+ bottoms of Case 1
substantially out performs the straight heavy cycle oil as a
catalytic cracker feed due to the hydrogenation of the polynuclear
aromatic rings, which took place in the hydrocracking phase.
* * * * *