U.S. patent number 3,622,499 [Application Number 05/004,806] was granted by the patent office on 1971-11-23 for catalytic slurry process for black oil conversion with hydrogen and ammonia.
This patent grant is currently assigned to Universal Oil Products Company. Invention is credited to Laurence O. Stine, Frank Stolfa.
United States Patent |
3,622,499 |
Stine , et al. |
November 23, 1971 |
CATALYTIC SLURRY PROCESS FOR BLACK OIL CONVERSION WITH HYDROGEN AND
AMMONIA
Abstract
A catalytic slurry process for effecting the conversion of a
hydrocarbonaceous charge stock containing asphaltenes and metallic
contaminants. The slurry constitutes charge stock, hydrogen, from
about 1.0 to about 25.0 percent by weight of finely divided
catalyst particles and, in a preferred embodiment, a portion of the
previously produced product effluent. Preferred catalysts are the
unsupported sulfides of the metals from Groups V-B, VI-B and VIII.
Prior to an initial separation, hydrogen sulfide is commingled with
the product effluent in order to convert the metals contained
therein to the sulfides thereof.
Inventors: |
Stine; Laurence O. (Western
Springs, IL), Stolfa; Frank (Park Ridge, IL) |
Assignee: |
Universal Oil Products Company
(Des Plaines, IL)
|
Family
ID: |
21712618 |
Appl.
No.: |
05/004,806 |
Filed: |
January 22, 1970 |
Current U.S.
Class: |
208/108; 208/97;
208/215; 208/102; 208/251H |
Current CPC
Class: |
C10G
49/22 (20130101); C10G 45/16 (20130101) |
Current International
Class: |
C10G
45/02 (20060101); C10G 45/16 (20060101); C10G
49/00 (20060101); C10G 49/22 (20060101); B01j
011/74 (); C10g 013/06 (); C10g 023/16 () |
Field of
Search: |
;208/108,215
;252/414,439 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Gantz; Delbert E.
Assistant Examiner: Schmitkons; G. E.
Claims
We claim as our invention:
1. A process for converting an asphaltene-containing
hydrocarbonaceous charge stock which comprises the steps of:
a. forming a reactive slurry of said charge stock, hydrogen,
ammonia and a finely divided catalyst containing at least one metal
component from the metals of Groups V-B, VI-B and VIII;
b. reacting said slurry in a reaction zone, or coil, at cracking
conditions including a pressure above about 500 p.s.i.g. and a
temperature above about 800.degree. F.;
c. separating the resulting cracked product effluent, in a first
separation zone, at substantially the same pressure and a
temperature below about 900.degree. F., to provide a first vaporous
phase and a first catalyst-containing liquid phase;
d. separating said first vaporous phase in a second separation
zone, at substantially the same pressure and a temperature in the
range of about 60.degree. to about 140.degree. F., to provide a
second liquid phase and a second vaporous phase, recycling at least
a portion of the latter to combine with said charge stock and
hydrogen;
e. separating at least a portion of said first catalyst-containing
liquid phase and said second liquid phase in a third separation
zone, at a reduced pressure of from atmospheric to about 100
p.s.i.g., to provide a first distillable product stream and a third
catalyst-containing liquid phase; and,
f. separating said third catalyst-containing liquid phase in a
fourth separation zone, at a temperature above about 700.degree. F.
and at subatmospheric pressure, to provide a second distillable
product stream and an asphaltene/catalyst sludge.
2. The process of claim 1 further characterized in that said
catalyst is an unsupported sulfide of at least one of the metals
from Groups V-B, VI-B and VIII.
3. The process of claim 1 further characterized in that said
catalyst constitutes from 1.0 to about 25.0 percent by weight of
said charge stock, as the elemental metal.
4. The process of claim 2 further characterized in that said
catalyst is an unsupported vanadium sulfide.
5. The process of claim 1 further characterized in that hydrogen
sulfide is commingled with said cracked product effluent in an
amount of from 1.0 to about 25.0 percent by weight, as elemental
sulfur.
6. The process of claim 1 further characterized in that said
reactive slurry contains from 0.5 to about 10.0 percent by weight
of ammonia.
7. The process of claim 1 further characterized in that said slurry
is reacted at a pressure from 1,000 to about 3,000 p.s.i.g. and a
temperature in the range of from 825.degree. to about 1,000.degree.
F.
Description
The process described herein is applicable to the conversion of
petroleum crude oil residuals having a high metals content and
comprising a hydrocarbon-insoluble asphaltene fraction. More
specifically, our invention is directed toward a method for
effecting a catalytic slurry process, in the presence of hydrogen,
in order to convert atmospheric tower bottoms, vacuum column
bottoms, crude oil residuals, topped and/or reduced crude oils,
coal oil extracts, crude oils extracted from tar sands, etc., all
of which are commonly referred to in the art as "black oil."
Petroleum crude oils, and particularly the heavy residuals derived
therefrom, contain sulfurous compounds in exceedingly large
quantities, nitrogenous compounds, high molecular weight
organometallic complexes principally comprising nickel and vanadium
as the metallic component and hydrocarbon-insoluble asphaltenic
material. The latter is generally found to be complexed with
sulfur, and, to a certain extent, with the metallic contaminants. A
black oil is generally characterized in petroleum technology as a
heavy hydrocarbonaceous material of which more than about 10.0
percent (by volume) boils above a temperature of about
1,050.degree. F. (referred to as nondistillables) and which further
has a gravity generally less than 20.0.degree. API. Sulfur
concentrations are exceedingly high, most often in the range of
about 2.0 to about 6.0 percent by weight. Conradson carbon residual
factors exceed 1.0 percent by weight and the concentration of
metals can range from as low as about 20 p.p.m. to as high as about
750 p.p.m. by weight.
The process encompassed by the present invention is particularly
directed toward the conversion of those black oils contaminated by
large quantities of insoluble asphaltenes and having a high metals
content--i.e. containing more than about 150 p.p.m. by weight.
Specific examples of the charge stocks to which our invention is
adaptable include a vacuum tower bottoms product having a gravity
of 7.1.degree. API and containing 4.1 percent by weight of sulfur
and 23.7 percent by weight of heptane-insoluble materials; a
"topped" Middle-East crude oil having a gravity of 11.0.degree. API
and containing about 10.1 percent by weight of asphaltenes and 5.2
percent by weight of sulfur; and, a vacuum residuum having a
gravity of 8.8.degree. API, containing 3.0 percent by weight of
sulfur and 4,300 p.p.m. by weight of nitrogen.
The utilization of our invention affords the conversion of such
material into distillable hydrocarbons, heretofore having been
considered virtually impossible to achieve on a continuous basis
with an acceptable catalyst life. The principal difficulty,
encountered in a fixed-bed catalytic system, resides in the lack of
sufficient catalyst stability in the presence of relatively large
quantities of metals--i.e. from about 150 p.p.m. to as high as 750
p.p.m., computed as the elements--and, additionally from the
presence of large quantities of asphaltenic material and other
nondistillables. The asphaltic material comprises high molecular
weight coke precursors, insoluble in light hydrocarbons such as
propane, pentane and/or heptane. The asphaltic material is
generally found to be dispersed within the black oil, and, when
subjected to elevated temperature, has the tendency to flocculate
and polymerize whereby conversion to more valuable oil-soluble
products becomes extremely difficult.
Candor compels recognition of the fact that many slurry-type
processes have been proposed. Regardless of the various operating
and processing techniques, the principal difficulty resides in the
separation of the effluent to provide substantially catalyst-free
distillable product, internal catalyst recirculation and "spent"
catalyst withdrawal. Success has been achieved primarily through
the use of intricate equipment at prohibitively high costs. An
obvious alternative is to utilize the black oil as the charge to a
coking unit for the production of coke and distillable
hydrocarbons. In view of the steadily increasing demand for
distillable hydrocarbons, particularly motor fuels, jet fuels and
stocks for conversion into liquefied petroleum gas, coking is no
longer suitable due to its relatively low yield of distillable
hydrocarbons. Our invention affords a more economical and less
difficult process from the standpoint of the desired product
recovery, internal catalyst recirculation and catalyst
withdrawal.
Therefore, in one embodiment, our invention provides a process for
converting an asphaltene-containing hydrocarbonaceous charge stock
which comprises the steps of: (a) forming a reactive slurry of said
charge stock, hydrogen, ammonia and finely divided catalyst
containing at least one metal component from the metals of Groups
V-B, V-B and VIII; (b) reacting said slurry in a reaction zone, or
coil, at cracking conditions including a pressure above about 500
p.s.i.g. and a temperature above about 800.degree. F.; (c)
separating the resulting cracked product effluent, in a first
separation zone, at substantially the same pressure and a
temperature below about 900.degree. F., to provide a first vaporous
phase and a first catalyst-containing liquid phase; (d) separating
said first vaporous phase in a second separation zone, at
substantially the same pressure and a temperature in the range
about 60.degree. to about 140.degree. F., to provide a second
liquid phase and a second vaporous phase, recycling at least a
portion of the latter to combine with said charge stock and
hydrogen; (e) separating said first catalyst-containing liquid
phase and said second liquid phase in a third separation zone, at a
reduced pressure from atmospheric to about 100 p.s.i.g., to provide
a first distillable product stream and a third catalyst-containing
liquid phase; and, (f) separating said third catalyst-containing
liquid phase in a fourth separation zone, at a temperature above
about 700.degree. F. and at subatmospheric pressure to provide a
second distillable product stream and an asphaltene/catalyst
sludge.
Other embodiments of our invention are directed toward particular
operating techniques and preferred ranges of operating variables
and conditions. Thus, the process is further characterized, in
another embodiment, in that at least a portion of said first
catalyst-containing liquid stream is recycled to combine with the
charge stock. The catalyst concentration, within the slurry being
introduced into the reaction chamber, is in the range of from about
1.0 to about 25.0 percent by weight, based upon fresh feed charge
stock, and preferably from about 2.0 percent to about 15.0 percent.
In a preferred embodiment, the process is further characterized in
that said reactive slurry contains from 0.5 to about 10.0 percent
by weight of ammonia. Since it is preferred to conduct the
conversion in the substantial absence of hydrogen sulfide in the
reaction zone, ammonia is injected, preferably in the recycled
gaseous phase, in sufficient quantity to neutralize the hydrogen
sulfide liberated during the course of the reaction. Hydrogen
sulfide is then commingled with the reaction zone effluent in order
to convert the catalytic metals to the sulfides.
SUMMARY OF INVENTION
The particular finely divided, solid catalyst utilized in the
present slurry process, is not considered to be essential. However,
it must be recognized that the catalytically active metallic
component of the catalyst necessarily possesses both cracking and
hydrogenation activity. In most applications of our invention, the
catalytically active metallic component or components will be
selected from the metals of Groups V-B, VI-B and VIII of The
Periodic Table. Thus, in accordance, with The Periodic Table of The
Elements, E. H. Sargent and Company, 1964, the preferred metallic
components are vanadium, chromium, iron, cobalt, nickel, niobium,
molybdenum, tantalum and/or tungsten. The noble metals of Group
VIII, namely ruthenium, rhodium, palladium, osmium, iridium, and
platinum, are not generally considered for use in a slurry-type
process in view of the economic considerations involved with these
relatively expensive metals. The foregoing metallic components may
be combined with a refractory inorganic oxide carrier material,
including alumina, silica, zirconia, magnesia, titania mixtures of
two or more, etc., the final composite being reduced to a finely
divided state. In such a composite, the active metallic components
may exist in some combined form such as the oxide, sulfide,
sulfate, carbonate, etc. Recent investigations and developments in
catalytic slurry processing of heavy hydrocarbon charge stocks have
indicated that the sulfides of the foregoing metals, and
particularly those of Group V-B, offer more advantageous results.
Furthermore, the process appears to be facilitated when the sulfide
of the metal is unsupported, as contrasted to being combined with a
refractory inorganic oxide carrier material. For this reason, the
preferred unsupported catalyst for use in the process of the
present invention, comprises tantalum, niobium or vanadium with a
vanadium sulfide being particularly preferred. In the interest of
brevity, the following discussion will be limited to the use of
vanadium sulfides, in an amount of about 1.0 to about 25.0 percent
by weight, as the catalyst in the present slurry process.
Regardless, of the character of the catalyst, it may be prepared in
any suitable, convenient manner, the precise method not being
essential to the present invention. For example, vanadium sulfides
may be prepared by reducing vanadium pentoxide with sulfur dioxide,
sulfuric acid and water to yield a solid hydrate of vanadyl
sulfate. The latter is treated with hydrogen sulfide at a
temperature of about 300.degree. C. to form vanadium tetrasulfide.
Reducing the vanadium tetrasulfide in hydrogen, at a temperature of
above about 300.degree. C., produces the vanadium sulfide which is
slurried into the system. As hereinbefore set forth, the
concentration of vanadium sulfide is preferably within the range of
about 2.0 to about 15.0 percent by weight, calculated as the
elemental metal. Excessive concentrations do not appear to enhance
the results, even with extremely contaminated charge stocks having
exceedingly high asphaltene contents.
DESCRIPTION OF DRAWING
In the accompanying drawing, illustrating one embodiment of our
invention, a simplified flow diagram is presented. Details such as
pumps, instrumentation and controls, heat-exchange and
heat-recovery circuits, valving, startup lines and similar hardware
have been omitted; these are considered to be nonessential to an
understanding of the techniques involved. The utilization of such
miscellaneous appurtenances, to modify the illustrated process
flow, are well within the purview of those skilled in the art.
Similarly, it is understood that the charge stock, operating
conditions, catalysts, design of fractionators, separators and the
like are exemplary only, and may be varied widely without departure
from the spirit of our invention, the scope of which is defined by
the appended claims.
With reference now to the drawing, the fresh feed charge stock, for
example a reduced crude oil, enters the process by way of line 1.
The charge stock is commingled with a hydrogen-rich recycle stream
from line 3 and a vanadium sulfide catalyst-containing hot recycle
stream from line 2. The mixture continues through line 1 into
reaction coil 6 at a pressure above about 500 p.s.i.g. and a
temperature above about 800.degree. F.; preferred conditions are a
pressure from 1,000 to about 3,000 p.s.i.g. and a temperature in
the range of from 825.degree. to about 1,000.degree. F. The
hydrogen concentration, within the reactive slurry entering
reaction coil 6, including makeup hydrogen introduced by way of
line 4 is from 1,000 to about 50,000 s.c.f./bbl., and preferably
from about 3,000 to about 20,000 s.c.f./bbl. In a preferred
embodiment, the reactive slurry also contains from 0.5 to about
10.0 percent by weight of ammonia introduced into the hydrogen-rich
recycle stream through line 5.
The product effluent from reaction coil 6 is admixed with from 1.0
to about 25.0 percent by weight of hydrogen sulfide from line 8,
and the mixture continues through line 7 into hot separator 9, at
substantially the same pressure as it emanates from reaction coil
6. Prior to being introduced into hot separator 9, the hydrogen
sulfide-containing reaction coil effluent is utilized as a
heat-exchange medium to lower its temperature to a level in the
range of from about 700.degree. to about 900.degree. F. Hot
separator 9 serves the principal function of providing a
principally vaporous phase, line 10, and a catalyst-containing
liquid phase, line 16, the latter containing primarily those
hydrocarbons boiling above a temperature of about 650.degree. F.
The vaporous phase in line 10 is cooled and condensed to a
temperature in the range of about 60.degree. to about 140.degree.
F., and introduced into receiver 11. The liquid phase in line 16
may be recycled, at least in part, by way of line 2 to combine with
the fresh feed charge stock in line 1. Since hydrogen sulfide has
been commingled with the reaction zone effluent, prior to
separation in hot separator 9, the catalyst being recycled by way
of line 2, with the hot separator liquid phase, is in the form of a
sulfide. The quantity so recycled is such that the combined liquid
feed ratio to reaction coil 6 is within the range of about 1.1 to
about 6.0. High-pressure receiver 11 provides hydrogen-rich
vaporous phase, being withdrawn by way of line 12, which vaporous
phase is introduced into hydrogen sulfide removal system 13. The
enriched hydrogen stream is recycled through line 3 by way of
compressive means not illustrated in the drawing, and is admixed
with makeup hydrogen in line 4 and ammonia from line 5. Hydrogen
sulfide is withdrawn from the removal system by way of line 14, at
least a portion of which is diverted through line 8 to combine with
the reaction product effluent in line 7.
That portion of the catalyst-containing liquid phase from hot
separator 9 not being recycled by way of line 2, continues through
line 16 into flash fractionator 17. Similarly, the liquid phase
from high-pressure receiver 11 is withdrawn by way of line 15 and
introduced into flash fractionator 17, preferably at a locus above
that through which the hot separator liquid is introduced. The
separation in flash fractionator 17 is effected at a reduced
pressure of from atmospheric to about 100 p.s.i.g. and a reboiler,
or bottom temperature in the range of 600.degree. to about
800.degree. F. In the drawing, flash fractionator 17 is shown as
separating the product into three individual streams. For the
purposes of this illustration, a naphtha fraction, having an end
boiling point of about 400.degree. F., and containing normally
gaseous hydrocarbons, is withdrawn through line 18. A gas oil
fraction, boiling up to a temperature of about 650.degree. F., is
withdrawn through line 19, while a heavier fraction, containing
catalyst particles and unreacted asphaltenes is withdrawn through
line 20. The latter is introduced into vacuum column 21 wherein
separation is effected to provide a light vacuum gas oil in line
22, a heavy vacuum gas oil in line 23 and, an asphaltene/catalyst
sludge in line 24. In one embodiment, not illustrated in the
drawing, vacuum column 21 is operated in a manner which provides a
slop-wax cut which is recycled to the reaction coil in admixture
with a portion of the asphaltene/catalyst sludge. When this
embodiment is practiced, a recycle stream from hot separator 9 is
generally not effected. The asphaltene/catalyst sludge may be
subjected to a series of filtration and washing techniques,
utilizing a suitable solvent to remove residual, soluble
hydrocarbons therefrom. The remainder of the sludge is generally
burned in air, resulting in vanadium pentoxide which is
subsequently reduced with sulfur dioxide, sulfuric acid and water
to produce vanadyl sulfate. The procedure then follows the
previously described scheme for the preparation of fresh vanadium
sulfide.
DESCRIPTION OF A PREFERRED EMBODIMENT
This illustration of a preferred embodiment will be presented in
connection with a commercially scaled unit designed to process
25,000 bbl./day of a Laguna reduced crude having a gravity of about
9.8.degree. API. Other characteristics of the charge stock include
an initial boiling point of 560.degree. F., a 10.0 percent
volumetric distillation temperature of 700.degree. F. and a 50.0
percent volumetric distillation temperature of 1,000.degree. F.;
the crude contains about 5,190 p.p.m. by weight of nitrogen, 9.6
percent by weight of heptane-insoluble asphaltenes, 2.8 percent by
weight of sulfur, about 438 p.p.m. of vanadium and 74 p.p.m. of
nickel, has a carbon/hydrogen atomic ratio of about 7.95 and an
average molecular weight of about 598.
The reduced crude, in an amount of about 696 mols./hr., is admixed
with 208 mols/hr. of ammonia, 13,865 mols/hr. of a hydrogen-rich
recycled gaseous phase (12,336 mols/hr. of hydrogen) and a hot
liquid recycle in an amount to result in a combined liquid feed
ratio of 2.0. The total charge, containing about 5.5 percent by
weight of a vanadium sulfide, is introduced into a reaction coil at
a pressure of about 2,000 p.s.i.g. and a temperature of about
850.degree. F. About 14 mols/hr. of hydrogen sulfide are added to
the reaction coil effluent prior to the introduction thereof into a
hot separator at a temperature of about 750.degree. F. The
separation effected in the hot separator is illustrated in table I,
with reference being made to line numbers in the accompanying
drawing. For convenience, the values are expressed in mols/hr. Not
included are 208 mols/hr. of neutralized hydrogen sulfide.
---------------------------------------------------------------------------
TABLE I: HOT SEPARATOR STREAM ANALYSES
Component Line 10 Line 16
__________________________________________________________________________
Ammonia 25 2 Hydrogen 8,747 476 Methane 1,532 126 Ethane 95 82
Propane 86 53 Butanes 55 20 Pentane-400.degree. F. 237 54
400.degree. -650.degree. F. 296 187 650.degree.- 1,050.degree. F.
60 430 Residuum -- 30
__________________________________________________________________________
The vaporous phase from the hot separator is cooled and condensed,
and passed into a high-pressure (about 1,900 p.s.i.g.) receiver at
a temperature of about 100.degree. F. A hydrogen-rich vaporous
phase is recycled therefrom to the reaction coil. The normally
liquid stream from the receiver is introduced into a flash
fractionator functioning at a temperature of 750.degree. F. and a
pressure of 75 p.s.i.g. The hot separator liquid stream is also
introduced into the flash fractionator, but through a locus below
that through which the receiver stream is introduced. The
separation effected in the cold receiver is presented in the
following table II:
---------------------------------------------------------------------------
table ii: cold receiver stream analyses
component Line 12 Line 15
__________________________________________________________________________
Hydrogen 8,611 136 Methane 1,406 126 Ethane 71 24 Propane 43 43
Butanes 13 42 Pentane-400.degree. F. -- 235 400.degree.-
650.degree. F. -- 296 650.degree.- 1,050.degree. F. -- 60 Residuum
-- --
__________________________________________________________________________
In this illustration, the flash fractionator provides an overhead
stream containing hexanes and lower-boiling components, a side-cut
naphtha stream of heptanes and other hydrocarbons boiling up to
400.degree. F., a light gas oil cut and a bottoms,
catalyst-containing stream comprising 650.degree. F.-plus
hydrocarbons. The latter is introduced into a vacuum column (55 mm.
of Hg.) at a temperature of 800.degree. F. A heavy vacuum gas oil
is recovered and an asphaltene/catalyst sludge is removed to a
catalyst recovery system.
The overall yields and product distribution are presented in the
following table III:
---------------------------------------------------------------------------
table iii: product distribution and yields
component Mols/Hr.
__________________________________________________________________________
Hydrogen 612 Methane 252 Ethane 106 Propane 96 Butanes 62 Pentanes
32 Hexanes 44 Heptane-400.degree. F. 213 400.degree.- 650.degree.
F. 483 650.degree.- 1,050.degree. F. 490 Residuum 30
__________________________________________________________________________
The foregoing specification indicates the method by which the
process encompassed by our invention is effected, and illustrates
the benefits afforded through the utilization thereof.
* * * * *