U.S. patent number 3,617,502 [Application Number 04/771,250] was granted by the patent office on 1971-11-02 for desulfurization and conversion of hydrocarbonaceous black oils.
This patent grant is currently assigned to Universal Oil Products Company. Invention is credited to Laurence O. Stine, Frank Stolfa.
United States Patent |
3,617,502 |
Stolfa , et al. |
November 2, 1971 |
DESULFURIZATION AND CONVERSION OF HYDROCARBONACEOUS BLACK OILS
Abstract
A process for converting asphaltene-containing hydrocarbonaceous
black oils into lower boiling, normally liquid hydrocarbon
products. The process involves the integration of a thermal
cracking coil and fixed-bed catalytic hydrogenation and
desulfurization, and is especially applicable to sulfurous charge
stocks containing less than 150 p.p.m. of metallic contaminants,
and more than about 10.0 percent by volume of nondistillables. The
charge stock is initially subjected to fixed-bed catalytic
desulfurization and hydrogenation, and a series of separation steps
to concentrate that portion of the reaction zone product boiling at
temperatures above the normal gasoline boiling range. This
high-boiling concentrate is then subjected to a noncatalytic,
thermal cracking reaction zone or coil.
Inventors: |
Stolfa; Frank (Park Ridge,
IL), Stine; Laurence O. (Western Springs, IL) |
Assignee: |
Universal Oil Products Company
(Des Plaines, IL)
|
Family
ID: |
25091208 |
Appl.
No.: |
04/771,250 |
Filed: |
October 28, 1968 |
Current U.S.
Class: |
208/89; 208/100;
208/102; 208/61 |
Current CPC
Class: |
C10G
49/22 (20130101); C10G 69/06 (20130101) |
Current International
Class: |
C10G
69/06 (20060101); C10G 69/00 (20060101); C10G
49/00 (20060101); C10G 49/22 (20060101); C10g
037/04 () |
Field of
Search: |
;208/61,89,100,102,57,58 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Gantz; Delbert E.
Assistant Examiner: Bruskin
Claims
We claim as our invention:
1. A process for the conversion of a sulfurous, hydrocarbonaceous
charge stock, of which at least about 10.0 percent boils above a
temperature of about 1,050.degree. F., into desulfurized
lower-boiling hydrocarbon products, which process comprises the
steps of:
a. heating said charge stock to a temperature of from 500.degree.
to about 775.degree. F., reacting said charge stock with hydrogen
in a catalytic reaction one, in contact with a catalytic composite
and at a pressure above about 1,000 p.s.i.g.
b. separating the resulting reaction zone effluent, in a first
separation one, at substantially the same pressure imposed upon
said first reaction one, and at a temperature of 700.degree. to
about 775.degree. F., to provide a first vapor phase and a first
liquid phase;
c. separating said first vapor phase, in a second separation one,
at substantially the same pressure imposed upon said first
separation one and at a reduced temperature, to provide a second
vapor phase rich in hydrogen, and a second liquid phase;
d. recycling at least a portion of said second vapor phase to said
first reaction one;
e. separating at least a portion of said first liquid phase, in a
third separation zone at substantially the same temperature, and a
reduced pressure of 150 to about 350 p.s.i.g. to provide a third
vapor phase and a third liquid phase;
f. cracking at least a portion of said third liquid phase in a
noncatalytic, thermal reaction zone
g. separating the resulting cracked product effluent, in a fourth
separation zone, at a reduced pressure of form atmospheric to about
100 p.s.i.g. to provide a fourth liquid phase and a fourth vapor
phase; and,
h. further separating said fourth liquid phase, in a fifth
separation zone, at a reduced pressure of from subatmospheric to
about 50 p.s.i.g. to provide an asphaltic residuum and a fifth
liquid phase containing distillable hydrocarbons of decreased
sulfur content.
2. The process of claim 1 further characterized in that a portion
of said fifth liquid phase is recycled to combine with said third
liquid phase, to provide a combined feed ratio to said thermal
reaction one of from about 1.2:1 to about 3.0:1.
3. The process of claim 1 further characterized in that said first
liquid phase is in part recycled to combine with said charge stock
to provide a combined feed ratio to said first reaction one of from
about 1.1:1 to about 3.5:1.
4. The process of claim 1 further characterized in that said charge
stock is heated to a temperature in the range of from about
650.degree. to about 775.degree. F.
5. The process of claim 1 further characterized in that said second
liquid phase and said third vapor phase are separated to recover a
normally liquid hydrocarbon stream containing gasoline boiling
range hydrocarbons.
6. The process of claim 1 further characterized in that a portion
of said fifth liquid phase is recycled to combine with the charge
stock to said catalytic reaction zone.
7. The process of claim 5 further characterized in that said second
liquid phase and said third vapor phase are combined and separated
to recover a normally liquid hydrocarbon stream containing gasoline
boiling range hydrocarbons.
8. The process of claim 1 further characterized in that the portion
of said third liquid phase is introduced, without intermediate
heating thereof, into said thermal reaction zone.
Description
APPLICABILITY OF INVENTION
The process described herein is primarily adaptable to the
desulfurization of petroleum crude oil residuals having relatively
low metals content-- i.e. containing less than 150 p.p.m. of total
metals. More specifically, the present invention is directed toward
a combination process for hydrogenating and desulfurizing
hydrocarbonaceous charge stocks which are commonly referred to as
"black oils." Petroleum crude oils, and particularly the heavy
residuals extracted from tar sands, topped or reduced crudes, and
vacuum residuals, contain high molecular weight sulfurous compounds
in exceedingly large quantities, nitrogenous compounds, asphaltic
material insoluble in light hydrocarbons such as pentane and/or
heptane, and high molecular weight organometallic complexes. With
respect to the metallic complexes, containing nickel and vanadium
as the metallic components, the various black oil charge stocks can
be classified as (1) "high metals" residuals, or (2) "low metals"
residuals. The present invention is primarily directed to the
processing of those hydrocarbonaceous black oils having low metals
content-- i.e. less than about 150 p.p.m. of total metals, computed
as if existing in the elemental state. A black oil charge stock is
generally characteried as a heavy carbonaceous material of which
more than about 10.0 percent by volume boils above a temperature of
1,050.degree. F. (referred to as nondistillables). Such material
generally has a gravity less than about 20.0.degree. API and sulfur
concentrations greater than about 2.0 percent by weight. With many
stocks, the sulfur concentration can range as high as about 5.0
percent by weight. Conradson carbon residue factors generally
exceed 1.0 percent by weight, and a great proportion of black oils
indicate a Conradson residue factor above 10.0.
Exemplary of those black oils, to the conversion and
desulfurization of which the present invention is directed, include
a crude tower bottoms product having a gravity of about
14.3.degree. API and contaminated by the presence of about 3.0
percent by weight of sulfur, 3,830 p.p.m. of total nitrogen, 85
p.p.m. of total metals, about 11.0 percent by weight of insoluble
asphaltenes, and about 41.0 percent nondistillables. The present
invention affords the conversion of such charge stocks into lower
boiling, normally liquid hydrocarbon products, and further converts
a considerable quantity of nondistillables. Additionally, the
normally liquid portion of the product effluent has been
substantially desulfurized to a level less than about 1.0 percent
by weight.
The principal difficulty, heretofore barring the attainment of an
economically feasible process, resides in the lack of sulfur
stability of catalytic composites when the charge stock is
characterized by the presence of large quantities of asphaltic
material and sulfur. This difficulty arises primarily as a
consequence of the necessity to effect the process at operating
severity levels such that nondistillable conversion simultaneously
takes place while sulfurous compounds are being converted into
hydrogen sulfide and hydrocarbons. Since the operation must be
effected at a high severity level, the asphaltic material,
dispersed within of charge stock, has the tendency to flocculate
and polymerize whereby the conversion thereof to more valuable
oil-soluble products is virtually precluded. Furthermore, the
polymerized asphaltic complexes become deposited upon the catalytic
composite, steadily increasing the rate at which the same becomes
deactivated.
The present invention is founded upon recognition of the fact that
acceptable desulfurization of low metals-containing black oils is
possible at relatively mild operating severities which favor
extended catalyst life without simultaneously effecting asphaltene
polymerization Hydrogenation reactions are enhanced at lower
severities, particularly with respect to temperature. In order that
the process becomes economically attractive from the standpoint of
producing the lower boiling, normally liquid hydrocarbon products,
an essential feature of the present invention is the subsequent
processing of the hydrogenated and desulfurized product effluent
from the fixed-bed catalytic reaction zone Therefore, as
hereinafter set forth in greater detail, the desulfurized catalytic
reaction effluent is separated to produce a hydrocarbon stream
boiling substantially completely above the gasoline boiling range,
which hydrocarbon stream is subsequently subjected to a
noncatalytic thermal reaction zone or coil.
OBJECTS AND EMBODIMENTS
A principal object of our invention is to provide an economical
process for effecting the desulfurization and conversion of
asphaltene-containing black oils to distillable hydrocarbons of
lower molecular weight. A corollary objective is to extend the
period of acceptable, economical catalyst life while desulfurizing
and hydrogenating hydrocarbonaceous black oils containing less than
about 150 p.p.m. of total metals.
Another object is to convert a sulfurous hydrocarbon charge stock,
a significant quantity of which exhibits a boiling range above a
temperature of 1,050.degree. F., into lower boiling distillable
hydrocarbons having a sulfur concentration less than about 1.0
percent by weight.
In one embodiment, therefore, our invention relates to a process
for the conversion of a sulfurous, hydrocarbonaceous charge stock,
of which at least about 10.0 percent boils above a temperature of
about 1,050.degree. F., into lower boiling hydrocarbon products,
which process comprises the steps of: (a) heating said charge stock
to a temperature of from 500.degree. F. to about 775.degree. F.,
reacting said charge stock with hydrogen in a first reaction zone,
in contact with the catalytic composite and at a pressure above
about 1,000 p.s.i.g.; (b) separating the resulting reaction zone
effluent, in a first separation zone, at substantially the same
pressure imposed upon said first reaction zone, to provide a first
vapor phase and a first liquid phase; (c) separating said first
vapor phase, in a second separation zone, at substantially the same
pressure imposed upon said first separation zone and at a reduced
temperature to provide a second vapor phase rich in hydrogen and a
second liquid phase; (d) recycling at least a portion of said
second vapor phase to said first reaction zone; (e) separating at
least a portion of said first liquid phase, in a third separation
zone, at substantially the same temperature, to provide a third
vapor phase and a third liquid phase; (f) cracking at least a
portion of said third liquid phase in a noncatalytic thermal
cracking zone, (g) separating the resulting cracked product
effluent in a fourth separation zone, at a reduced pressure of from
atmospheric to about 100 p.s.i.g. to provide a fourth liquid phase
and a fourth vapor phase; and, (h) further separating said fourth
liquid phase, in a fifth separation zone, at a reduced pressure of
from subatmospheric to about 50 p.s.i.g. to provide a fifth liquid
phase containing distillable hydrocarbons, and an asphaltic
residuum.
Other embodiments of our invention, as hereinafter set forth in
greater detail, reside primarily in preferred ranges for process
variables and in various processing techniques. For example, in
another embodiment, at least a portion of said fifth liquid phase
is recycled to combine with said third liquid phase, to provide a
combined feed ratio to said thermal reaction zone of from about
1.1:1 to about 4.5:1. . In a particularly preferred embodiment, the
fifth separation zone is a vacuum column which serves to
concentrate the unconverted asphaltic residuum and to provide at
least a heavy vacuum gas oil, a light vacuum gas oil and a slop-wax
cut. Generally, the latter, with or without a portion of the heavy
vacuum gas oil, is recycled to the thermal cracking coil. Where the
desired product distribution demands, a portion of the slop-wax cut
may be recycled to combine with the fresh black oil charge to the
fixed-bed reaction zone. The total charge to the first, fixed-bed
catalytic hydrogenation zone, including hydrogen recycle and makeup
required to maintain pressure and supplant that which is consumed
within the overall process, is heated to a temperature within the
range of from about 650.degree. to about 775.degree. F. The precise
temperature, to which the charge to the catalytic reaction one is
heated, is controlled within the aforesaid range by monitoring the
temperature of the reaction zone product effluent. Since the
principal reactions being effected are exothermic, a temperature
rise is experienced as the charge and hydrogen pass through the
catalyst bed. Economically acceptable catalyst life is achieved
when the maximum catalyst temperature, which is virtually the same
as that of the product effluent, is maintained at a maximum level
of about 800.degree. F. In another embodiment, the first reaction
zone effluent, being introduced into the first separation zone, is
at a temperature of from about 700.degree. to about 775.degree. F.
in order that the heavier constituents of the reaction zone product
effluent are not carried over into the principally vaporous phase.
Other objects and embodiments of our invention will be evident from
the following, more detailed description of the process encompassed
thereby.
SUMMARY OF INVENTION
As hereinbefore set forth, the principal function of the present
invention resides in the production of maximum quantities of
distillable hydrocarbons which have been substantially reduced with
respect to sulfur concentration. Through the utilization of the
present combination process, this is accomplished in a highly
economical fashion while avoiding the difficulties of currently
practiced processing techniques. Paramount is the extension of the
period of time during which the fixed-bed of the solid catalytic
composite functions in an acceptable manner. With respect to the
processing of "high metals" black oils, being those containing more
than about 150 p.p.m. of total metals, it has been found that a
successful operation involves initially visbreaking the fresh
hydrocarbon charge stock in the presence of limited quantities of
hydrogen. Although both technical and economical justification
exists to support this processing technique, there is incurred a
yield loss with respect to that quantity of the original
nondistillable asphaltics which are not converted by way of
catalytic processing. This yield loss results primarily from the
fact that thermal cracking, in the presence of hydrogen, does not
achieve the conversion of all the convertible asphaltics within the
charge stock, the unconverted portion of which is removed from the
system as an asphaltic residuum prior to subjecting the remainder
of the thermally cracked product effluent to further conversion in
the fixed-bed reaction zone. If the as-received high metals charge
stock were processed initially in the fixed-bed catalytic reaction
zone, the presence of exceedingly high concentrations of metals in
an environment conductive to effecting acceptable desulfurization,
results in extreme catalyst deactivation. In accordance with the
present process, primarily applicable to those charge stocks of low
metals content, the residual charge stock is catalytically
desulfurized, and at least partially converted, at relatively mild
hydrogenation severities which favor extended catalyst life. The
catalytically converted product effluent is subjected to a series
of separation steps in order to provide a liquid phase
substantially free from gasoline boiling range hydrocarbons. This
liquid phase is utilized as the charge to a noncatalytic thermal
reaction zone, or coil. As hereinafter indicated, in a specific
example integrated into the description of the drawing, this
particular process offers maximum production of distillable
hydrocarbons accompanied by maximum desulfurization of the charge
stock whose original metals content is less than about 150 p.p.m.
In a preferred embodiment, the total charge to the fixed-bed
catalytic reaction zone includes the fresh hydrocarbon charge
stock, a recycled hydrogen-rich gaseous phase, makeup hydrogen, and
a recycled diluent, the source of the latter being hereinafter set
forth. This mixture is raised to a temperature of from about
500.degree. to about 775.degree. F., as measured at the inlet to
the catalyst bed. In order to preserve catalyst stability, the
inlet temperature is controlled at a level such that the
temperature of the reaction product effluent, or the maximum
catalyst bed temperature, does not exceed about 800.degree. F. A
certain measure of temperature control, within the fixed-bed of
catalyst, is afforded through the conventional utilization of
either a quench hydrogen stream, or quench liquid, or both,
introduced at one or more intermediate loci of the catalyst bed.
The catalytic reaction zone is maintained under an imposed pressure
of from about 1,000 to about 4,000 p.s.i.g., and the hydrocarbon
charge stock contacts the catalyst at a liquid hourly space
velocity of from about 0.5 to 10.0, based upon the fresh
hydrocarbon charge stock exclusive of recycled diluent and/or any
quench streams employed for temperature control. The hydrogen
concentration will be in the range of from about 5,000 to about
50,000 standard cubic feet per barrel, while the combined feed
ratio, defined as total volumes of liquid charge per volume of
fresh hydrocarbon charge, is in the range from about 1.1:1 to about
3.5:1.
The catalytic composite disposed within the fixed-bed catalytic
reaction, or conversion zone, can be characterized as containing a
metallic component having hydrogenation activity, which component
is combined with a suitable refractory inorganic oxide carrier
material of either synthetic, or natural origin. The precise
composition and method of manufacturing the carrier material is not
considered essential to the present invention, although a siliceous
carrier, such as 88.0 percent by weight of alumina and 12.0 percent
by weight of silica, or 63.0 percent by weight of alumina and 37.0
percent by weight of silica are generally preferred. Suitable
metallic components having hydrogenation activity are those
selected from the group consisting of the metals of Groups VI-B and
VIII of the Periodic Table, as set forth in The Periodic Table of
The Elements, E. H. Sargent & Company, 1964. Thus, the
catalytic composite may comprise one or more metallic components
selected from the group of molybdenum, tungsten, chromium, iron,
cobalt, nickel, platinum, iridium, osmium, rhodium, ruthenium, and
mixtures and compounds thereof. The concentration of the catalytic
metallic component, or components, is primarily dependent upon the
particular metal as well as the characteristics of the charge
stock. For example, the metallic components of Group VI-B are
generally present in an amount within the range of from about 1.0
percent to about 20.0 percent by weight, the iron-group metals in
an amount within the range of about 0.2 percent to about 10.0
percent by weight, whereas the noble metals of Group VIII are
preferably present in an amount within the range of about 0.1
percent to about 5.0 percent by weight, all of which are calculated
as if these compounds existed within the catalytic composite in the
elemental state. The refractory inorganic carrier material, with
which the catalytic reactive metallic components are combined, may
comprise alumina, silica, zirconia, magnesia, Titania boria,
strontia, hafnia, and mixtures of two or more including
silica-alumina, alumina-silica-boron phosphate, silica-zirconia
silica-magnesia, silica-titania, alumina-zirconia,
alumina-magnesia, silica-alumina-titania,
alumina-magnesia-zirconia, silica-alumina-boria, etc. Before
further summarizing our invention, several definitions are believed
necessary in order that a clear understanding of the invention be
afforded. In the present specification and the appended claims, the
phrase "pressure substantially the same as" is intended to connote
the pressure under which a succeeding vessel is maintained,
allowing only for the pressure drop experienced as a result of the
flow of fluids through the system. For example, where the catalytic
first reaction zone is maintained at a pressure of about 2,800
p.s.i.g., the first separation zone, or "hot separator" will
function at about 2,680 p.s.i.g. Similarly, unless otherwise
specified, the phrase "temperature substantially the same as" is
employed to indicate that the only reduction in temperature stems
from normally experienced loss due to the flow of material from one
piece of equipment to another, or from the conversion of sensible
to latent heat by "flashing" where a pressure drop occurs. When
utilized, the term "hydrocarbons boiling within the gasoline
boiling range" is intended to connote those normally liquid
hydrocarbons boiling at temperatures up to about 400.degree. or
about 450.degree. F., including pentanes and heavier hydrocarbons,
and, as in some localities, butanes. Likewise, a commonly referred
to boiling range for gas oil is an initial boiling point of about
650.degree. F. and an end boiling point of about 1,050.degree. F.
The higher boiling 70.0 to about 80.0 percent thereof, the heavy
gas oil, characteristically is considered having an initial boiling
point of about 750.degree. F. It is, of course, recognized that a
"light gas oil" can have an initial boiling point as low as about
350.degree. F. and an end boiling point as high as about
800.degree. F. Similarly, the "heavy gas oil" can have an initial
boiling point as low as about 650.degree. F.
The total product effluent from the catalytic reaction zone, at a
maximum temperature of about 800.degree. F., is passed into a first
separation zone hereinafter referred to as the "hot separator." The
principal function served by the hot separator is to separate the
mixed-phase product effluent into a principally vaporous phase rich
in hydrogen and a principally liquid phase containing some
dissolved hydrogen. In a preferred embodiment, the total reaction
product effluent is utilized as a heat-exchange medium in order to
lower the temperature thereof to a level in the range of from about
700.degree. to about 775.degree. F., and preferably below the level
of 750.degree. F. The principally vaporous phase from the hot
separator is introduced into a second separation zone hereinafter
referred to as the "cold separator." The cold separator, operating
at substantially the same pressure as the hot separator, but at a
significantly lower temperature in the range of about 60.degree. to
about 140.degree. F., serves to concentrate the hydrogen in a
second principally vaporous phase. The hydrogen-rich vapor phase,
comprising about 82.5 mol percent hydrogen, and only about 2.3 mol
percent propane and heavier hydrocarbons, is made available for use
as a recycle stream to be combined with the fresh black oil charge
stock. Butanes and heavier hydrocarbons are condensed in the cold
separator, and removed therefrom in a second principally liquid
phase.
The first liquid phase from the hot separator may be in part
recycled to combine with the fresh hydrocarbon charge stock to
serve as a diluent for the heavier constituents thereof. The
quantity of the liquid phase diverted in this manner is such that
the combined feed ratio to the catalytic reaction zone, being
defined as total volumes of liquid charge per volume of fresh
liquid charge, is within the range of from about 1.1:1 to about
3.5:1. The remaining portion of the principally liquid phase from
the hot separator is introduced into a third separation one
hereinafter referred to as the "hot flash zone." The hot flash zone
functions at about the same temperature as the liquid phase
withdrawn from the hot separator, but at a significantly reduced
pressure of from about 150 to about 350 p.s.i.g. The principally
vaporous phase from the hot flash zone comprises primarily
hydrocarbons boiling below a temperature of about 650.degree. F.,
and containing a relatively minor quantity of hydrocarbons normally
considered to be within the heavy gas oil boiling range. This
principally vaporous stream may be combined with the liquid stream
from the cold separator, and the mixture introduced into a cold
flash zone at a pressure of from atmospheric to about 60 p.s.i.g.
and a temperature of from 60.degree. to about 140.degree. F.
The principally liquid phase withdrawn from the hot flash zone is
introduced into a thermal cracking reaction zone, or coil, at
substantially the same temperature, and a pressure of from about
150 to about 350 p.s.i.g. The thermally cracked product effluent,
at a temperature of from about 875.degree. to about 950.degree. F.,
and a pressure of from about 40 to about 100 p.s.i.g., is cooled to
a temperature of about 700.degree. F., and introduced into a fourth
separation zone hereinafter referred to as the "flash
fractionator." The liquid phase from the flash fractionator is
introduced into a vacuum column maintained at about 25 to about 75
mm. of Hg., absolute. The vacuum column serves as the fifth
separation zone, the principal function of which is the
concentration and separate recovery of an asphaltic residuum,
containing high molecular weight sulfurous compounds and being
substantially free from distillable hydrocarbons. In general, gas
oil streams are recovered from the vacuum column as a separate
light vacuum gas oil (LVGO) having a boiling range of from about
320.degree. to about 750.degree. F., a medium vacuum gas oil (MVGO)
boiling from about 750.degree. to about 980.degree. F., and a heavy
vacuum gas oil containing the remainder of the distillable
hydrocarbons. It is understood that the particular boiling ranges
of the various gas oil streams, recovered from the vacuum column,
are not essential to our invention, but will generally be
determined by various refinery and marketing demands. A preferred
technique is to separate a slop-wax cut, from the vacuum column,
which contains primarily these distillables boiling above
980.degree. F., but may consist of up to about 30.0 percent by
volume of the total distillables boiling above 750.degree. F.
Although a portion of the slop-wax cut may be recycled to the
catalytic hydrogenation/desulfurization reaction zone, it is
generally recycled to the thermal coil in order to increase the
yield of the more desirable gas oils. The amount of slop-wax so
recycled is such that the combined feed ratio to the thermal
reaction coil is above about 1.2:1 and generally not higher than
about 3.0:1.
The principal advantages, or benefits, attendant the use of our
invention, reside in (1) an extension of acceptable catalyst life
with respect to the fixed-bed catalytic reaction zone, which stems
primarily from the fact that desulfurization, to a level less than
about 1.0 percent by weight, is effected at a relatively low
severity of operation with the result that the atmosphere within
the reaction one is not conductive to the formation of polymer
products otherwise resulting from the presence of the
hydrocarbon-insoluble asphaltenes; (2) a significant reduction in
the required size of the vacuum flash column which, as will be
recognized by those having skill in the art of petroleum processing
techniques, affords an added advantage with respect to the overall
economics of the process; and, (3) increased yields of the more
valuable gas oils.
DESCRIPTION OF DRAWING
For the purpose of demonstrating the illustrated embodiment, and
the utilization therein of the process of the present invention,
the drawing will be described in connection with the conversion of
a vacuum column bottoms product having a gravity of 6.0.degree. API
and an ASTM 20.0 percent volumetric distillation temperature of
about 1,055.degree. F. In addition, the charge stock contains 4,000
p.p.m. of nitrogen, 5.5 percent by weight of sulfur, 100 p.p.m. of
nickel and vanadium, 6.0 percent by weight of heptane-insoluble
asphaltenes and has a Conradson carbon residue factor of 21.0
percent by weight. The description will be directed toward a
commercially scaled unit having a capacity of about 8,000 barrels
per stream day. In the drawing, the embodiment is presented by
means of a simplified flow diagram in which such details as pumps,
instrumentation and controls, heat-exchange and heat-recovery
circuits, valving, startup lines and similar hardware have been
omitted as nonessential to an understanding of the techniques
involved. The use of such miscellaneous appurtenances, to modify
the illustrated process flow, are well within the purview of those
skilled in the art. Similarly, it is further understood that the
charge stock, stream compositions, operating conditions, 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.
It is intended that the charge stock be converted into maximum
distillable hydrocarbons which are recoverable by ordinary
distillation techniques in commonly utilized fractionation systems.
The charge stock is processed in a fixed-bed catalytic
desulfurization and desulfurization zone in admixture with about
10,000 s.c.f./bl. of hydrogen, based upon fresh feed exclusive of
recycle streams, at a catalyst bed inlet temperature of about
700.degree. F., and a pressure of about 3,105 p.s.i.g. The liquid
hourly space velocity, based upon fresh feed only, is about 0.5,
and the combined liquid feed ratio is about 2.0:1.
With respect now to the drawing, the charge stock, in an amount of
about 7,678 bl./day (185.94 mols/hr.), is introduced into the
system by way of line 1, and following heat-exchange with various
hot effluent streams, is passed into heater 5 in admixture with a
recycled hydrogen-rich stream from line 3 and a hot separator
bottoms liquid recycle in line 2. Makeup hydrogen, from a suitable
external source, to maintain plant pressure, and to replace that
hydrogen consumed in the overall process, is introduced by way of
line 4. The total charge to the heater is at a temperature of about
500.degree. F.; this is increased to a level of about 700.degree.
F., as measured at the inlet to the catalyst bed. The thus-heated
total charge passes through line 6 into fixed-bed catalytic
reaction one 7. The catalyst disposed in reaction one 7 is a
composite of 88.0 percent by weight of alumina and 12.0 percent by
weight of silica, with which is combined 2.0 percent by weight of
nickel and about 16.0 percent by weight of molybdenum, calculated
as the elemental metals.
Component analyses of the total charge to reaction zone are
presented in table I. In the table, line 3 includes both recycled
and makeup hydrogen, line 2 is the liquid recycle from hot
separator 9 and line 1 represents the total charge.
---------------------------------------------------------------------------
TABLE I: Reaction one Charge
Line No. 3 2 1
__________________________________________________________________________
Component, mols/hr.
__________________________________________________________________________
Nitrogen 11.07 1.85 12.93 Hydrogen 8430.09 175.52 8605.61 Hydrogen
Sulfide 739.02 26.36 765.38
Methane 1119.04 31.82 1150.86 Ethane 133.14 7.53 140.67 Propane
67.56 4.17 71.73
Butanes 24.49 2.06 26.55 Pentanes 6.60 0.92 7.52 Hexanes 4.70 1.29
5.99
C.sub.7 -320.degree. F. 2.00 3.19 5.19 320.degree. - 520.degree. F.
0.24 11.23 11.47 520.degree. - 650.degree. F. 16.25 16.25
650.degree. - 750.degree. F. 22.75 22.75
750.degree. - 980.degree. f. 67.16 67.16 980.degree. f.-plus 9.27
9.27 Residuum 78.78 78.78 Charge Stock 185.94
__________________________________________________________________________
The conversion product effluent, in mixed phase in line 8, at a
temperature of about 800.degree. F., is utilized as a heat-exchange
medium, and is introduced into hot separator 9 at a temperature of
775` F. and a pressure of about 3,040 p.s.i.g. A principally
vaporous phase is withdrawn by way of line 10, and a principally
liquid phase via line 12. In the present specification, and in the
appended claims, the terms "principally vaporous" and "principally
liquid," are intended to describe a particular stream, the major
proportion of the components of which are either normally gaseous,
or normally liquid at standard conditions. At least a portion of
the liquid phase, withdrawn from hot separator 9, is diverted via
line 2 to combine with the fresh hydrocarbon charge stock, serving
as a diluent for the heavier constituents thereof. The quantity of
this recycled stream is 7,678 bl./day (460.15 mols/hr.), to provide
a combined liquid feed ratio of 2.0:1.
The separation of the reaction zone effluent, being effected in
separator 9, is presented in the following table II, wherein line 8
is the feed to the separator (or the reaction zone effluent), line
10 is the vaporous phase and line 12 is the net liquid phase
exclusive of the recycled portion in line 2.
---------------------------------------------------------------------------
TABLE II: Hot Separator Stream Analyses
Line No. 8 10 12 Component, mols/hr.
__________________________________________________________________________
Nitrogen 12.92 9.40 1.67 Hydrogen 7679.21 7345.65 158.04 Hydrogen
Sulfide 906.43 856.33 23.74
Methane 1188.95 1128.48 28.65 Ethane 160.61 146.30 6.78 Propane
89.52 81.59 3.76
Butanes 38.85 34.93 1.86 Pentanes 14.55 12.81 0.83 Hexanes 17.60
15.15 1.16
C.sub.7 -320.degree. F. 32.10 26.02 2.88 320.degree. - 520.degree.
F. 68.54 47.20 10.11 520.degree. - 650.degree. F. 51.51 20.62 14.63
650.degree. - 750.degree. F. 50.89 7.67 20.48
750.degree. - 980.degree. f. 129.45 1.81 60.47 980.degree. f.- plus
17.61 8.34 Residuum 149.72 70.94
__________________________________________________________________________
It will be noted, from table II, that the material in line 10 is
75.5 mol percent hydrogen, and comprises only about 1.35 mol
percent pentanes and heavier normally liquid hydrocarbons. It is
therefore, a principally vaporous phase. Likewise, the stream in
line 12 comprises about 19.9 mol percent butanes and lighter
material, exclusive of hydrogen which is dissolved in the heavier
hydrocarbons, and is considered, therefore, a principally liquid
phase.
That portion of the hot separator bottoms stream not diverted
through line 2, continues through line 12 into hot flash one 13. A
reduction in pressure is effected by means of a reducing valve not
indicated in the drawing, and the stream enters hot flash one 13 at
a pressure of about 250 p.s.i.g. and a temperature of about
768.degree. F. As hereinafter set forth, the principal function of
flash zone 13 is to concentrate the heavier components in a liquid
phase which serves as the charge to thermal cracking coil 17. As
seen in the following table III, the vaporous phase in line 14
comprises about 89.2 mol percent of material boiling below about
520.degree. F. exclusive of hydrogen, while the liquid stream in
line 16 comprises about 6.3 mol percent exclusive of hydrogen.
---------------------------------------------------------------------------
TABLE III: Hot Flash Zone Stream Analyses
Line No. 14 16
__________________________________________________________________________
Component, mols/hr.
__________________________________________________________________________
Nitrogen 1.45 0.22 Hydrogen 151.87 6.17 Hydrogen Sulfide 22.47
1.27
Methane 27.49 1.16 Ethane 6.15 0.63 Propane 3.36 0.40
Butanes 1.61 0.24 Pentanes 0.69 0.14 Hexanes 0.93 0.23
C.sub.7 -320.degree. F. 2.12 0.76 320.degree. -520.degree. F. 5.89
4.22 520.degree.- 650.degree. F. 4.73 9.90 650.degree. -
750.degree. F. 3.10 17.37
750.degree. - 980.degree. f. 1.92 58.55 980.degree. f.- plus 0.01
8.33 Residuum 70.94
__________________________________________________________________________
The liquid phase in line 16 is admixed with about 1.0 wt. percent
of 230 p.s.i.g. steam, and the mixture enters thermal coil 17 at a
temperature of about 740.degree. F. and a pressure of about 170
p.s.i.g. The thermally cracked produce effluent, at a pressure of
about 55 p.s.i.g. and a temperature of about 930.degree. F., and,
after being cooled, passes via line 18 into a rectified flash
fractionator 19 at a temperature of about 700.degree. F. and a
pressure of about 55 p.s.i.g. A vapor phase is withdrawn from flash
fractionator 19 through line 20, and a liquid phase through line
24. The latter is introduced into vacuum flash column 25 at a
temperature of about 750.degree. F. The vacuum column is
functioning at about 25 mm. of Hg., absolute through the
utilization of standard vacuum jets which are not illustrated in
the drawing. The separation effected in flash fractionator 18 is
presented in the following table IV, along with the component
analysis of the thermally cracked product effluent in line 18,
exclusive of water.
---------------------------------------------------------------------------
TABLE IV. Flash Fractionator Stream Analyses
Line No. 18 20 24
__________________________________________________________________________
Component, mols./hr.
__________________________________________________________________________
Nitrogen 0.22 0.22 Hydrogen 11.87 11.82 0.05 Hydrogen Sulfide 3.68
3.65 0.03
Methane 22.34 22.23 0.11 Ethane 16.93 16.70 0.23 Propane 22.40
21.92 0.48
Butanes 16.53 15.87 0.66 Pentanes 17.77 16.56 1.21 Hexanes 14.55
13.06 1.49
C.sub.7 -320.degree. F. 33.83 28.31 5.52 320.degree. - 520.degree.
F. 50.47 33.80 16.67 520.degree. - 650.degree. F. 30.33 10.29 20.04
650.degree. - 750.degree. F. 24.49 2.75 2.74
750.degree. - 980.degree. f. 56.88 0.26 56.62 980.degree. f.- plus
10.00 10.00 Residuum 39.41 39.41
__________________________________________________________________________
The principally vaporous phase withdrawn from hot separator 9
through line 10, is cooled to a temperature of about 120.degree.
F., and is introduced into cold separator 11 at a pressure of about
3,000 p.s.i.g. A hydrogen-rich gaseous phase is withdrawn through
line 3, and is recycled therethrough to combine with the fresh
hydrocarbon charge stock in line 1. A principally liquid phase is
withdrawn from cold separator 11 through line 15. The separation
effected in cold separator 11, exclusive of makeup hydrogen, is
presented in the following table V.
---------------------------------------------------------------------------
TABLE V: Cold Separator Stream Analyses
Line No. 3 15
__________________________________________________________________________
Component, mols/hr.
__________________________________________________________________________
Nitrogen 9.29 0.11 Hydrogen 7274.70 70.95 Hydrogen Sulfide 739.02
117.31
Methane 1091.19 37.29 Ethane 133.14 33.16 Propane 67.56 14.03
Butanes 24.49 10.44 Pentanes 6.60 6.21 Hexanes 4.70 10.45
C.sub.7 -320.degree. F. 2.00 24.02 320.degree. - 520.degree. F.
0.24 46.96 520.degree. - 650.degree. F. 20.62 650.degree. -
750.degree. F. 7.67
750.degree. - 980.degree. f. 1.81 980.degree. f.- plus Residuum
__________________________________________________________________________
Vacuum flash column 25 serves to concentrate the residuum, 39.41
mols/hr. leaving via line 28, and also to separate a light vacuum
gas oil (LVGO), line 26 and a heavy vacuum gas oil (HVGO), line 27.
The HVGO, having a boiling range of 750.degree. to 1,050.degree.
F., is in an amount of about 66.62 mols/hr., and the LVGO is in a
amount of 58.45 mols/hr. Lighter material boiling below 320.degree.
F. is removed from vacuum flash column 25 by the jets which are not
indicated in the drawing.
Cold flash zone 21 has been illustrated for the sake of
completeness, indicating the separation of the mixture of the hot
flash vapors (line 14), the flash fractionator vapors (line 20) and
the cold separator liquid (line 15). In a commercial installation,
the vapors from the flash fractionator would be recovered
separately due to the relatively high degree of olefinicity
thereof. Component analyses indicating the separation effected in
cold flash zone 21 are presented in the following table VI.
---------------------------------------------------------------------------
TABLE VI: Cold Flash Zone Stream Analyses
Line No. Feed 22 23
__________________________________________________________________________
Component, mols/hr.
__________________________________________________________________________
Nitrogen 1.78 1.78 Hydrogen 234.64 232.53 2.11 Hydrogen Sulfide
143.43 96.75 46.68
Methane 87.01 82.63 4.38 Ethane 56.01 47.12 8.89 Propane 39.31
26.24 13.07
Butanes 27.92 11.87 16.05 Pentanes 23.46 4.84 18.62 Hexanes 24.44
2.54 21.90
C.sub.7 -320.degree. F. 54.45 1.86 52.59 320.degree. -520.degree.
F. 86.65 0.05 86.60 520.degree. -650.degree. F. 35.64 35.64
650.degree. -750.degree. F. 13.52 13.52
750.degree. -980.degree. f. 3.99 3.99 980.degree. f.- plus 0.01
0.01 Residuum
__________________________________________________________________________
Normally gaseous material is removed via line 22 to a light ends
recovery system, while normally liquid hydrocarbons, including
butanes, are removed via line 23 for further separation by
fractionation
The overall product yields, exclusive of normally gaseous material,
but inclusive of butanes and the normally liquid hydrocarbons
recoverable from the vacuum jets and light ends recover (line 22),
are presented in the following table VII.
---------------------------------------------------------------------------
TABLE VII: Overall Product Yields
Component Mols/hr.
__________________________________________________________________________
Butanes 28.58 Pentanes 24.67 Hexanes 25.93
C.sub.7 -320 F. 59.97 320.degree. -520.degree. F. 103.32
520.degree. -650.degree. F. 55.68 650.degree. -750.degree. F.
35.26
750.degree. -980.degree. F. 60.61 980.degree. F.-Plus 10.01
Residuum 39.41
__________________________________________________________________________
The sulfur concentration of the distillable hydrocarbon products is
about 0.83 percent by weight.
In a process in which the thermal coil is not an integral part, the
fixed-bed catalytic reaction one must necessarily be operated at a
significantly higher severity level in order to produce the maximum
quantity of distillables. The use of the present process affords a
reduction in operating severity, as measured by the catalyst bed
inlet temperature, of from 50.degree. to as much as 100.degree. F.
With respect to extending the period of time during which the
catalytic composite functions in an economically acceptable manner,
without experiencing deactivation, the present process increases
catalyst life (expressed as barrels per pound) from 50 to 80
percent, resulting in longer on-stream cycles. A reduction in the
size of the vacuum column, from a nominal diameter of 11.0 to 8.6
feet, is made possible. This, as will be noted by those skilled in
the art of petroleum processing techniques, affords a significant
reduction in capital outlay for equipment.
The foregoing specification, and especially the example integrated
within the description of the drawing, clearly illustrates the
process of our invention and indicates the benefits afforded
through the utilization thereof.
* * * * *