CA 02637421 2008-07-10
Title: Upgrading of bitumen using SuperCritical Wet Oxidation
The present relates to the use of "supercritical water oxidation" to burn a
portion of
bitumen, heavy oil or the like (i.e. any hydrocarbon type material having a
low API e.g.
an API of 16 or less) in order to provide heat to the remaining bitumen, heavy
oil or the
like so as to raise the temperature thereof to a cracking temperature for
upgrading the
bitumen, heavy oil or the like to a (more) pumpable product for transfer to a
downstream
refinery. The upgrading involves subjecting the remaining bitumen, heavy oil
or the like
to cracking conditions to produce (in situ) material(s) of smaller molecular
weight which
may act as diluent type material(s) so as to obtain a cracked product (e.g.
API 20 -30)
which is not only relatively better suited for being pumped than the starting
bitumen,
heavy oil or the like but which as desired or necessary may have a reduced
mineral
content.
The American Petroleum Institute gravity, or API gravity (herein sometimes
referred to
simply as API), is a measure of how heavy or light a petroleum liquid is
compared to
water. If its API gravity is greater than 10, it is lighter and floats on
water; if less than 10,
it is heavier and sinks. API gravity is thus a measure of the relative density
of a petroleum
liquid and the density of water, but it is used to compare the relative
densities of
petroleum liquids. For example, if one petroleum liquid floats on another and
is therefore
less dense, it has a greater API gravity. Although mathematically API gravity
has no
units, it is nevertheless referred to as being in "degrees". API gravity is
graduated in
degrees on a hydrometer instrument and was designed so that most values would
fall
between 10 and 70 API gravity degrees.
Generally speaking 40 to 45 API gravity degree oils have a greatest commercial
price and
values outside this range have lower commercial price. Above 45 degrees API
gravity the
molecular chains become shorter and less valuable to a refinery.
Crude oil is classified as light, medium or heavy, according to its measured
API gravity.
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CA 02637421 2008-07-10
Light crude oil is defined as having an API gravity higher than 31.1 API
Medium oil is defined as having an API gravity between 22.3 API and 31.1 API
Heavy oil is defined as having an API gravity below 22.3 API.
Simply put, bitumen sinks in fresh water, while oil floats.
Crude oil with API gravity less than 10 API is referred to as extra heavy oil
or bitumen.
Bitumen derived from the oil sands deposits in the Alberta, Canada area has an
API
gravity of around 8 API. It is 'upgraded' to an API gravity of 31 API to 33
API and the
upgraded oil is known as synthetic crude.
The following, by way of example only will in particular relate to bitumen
upgrading
which may for example be carried out on site at a bitumen field wherein the
bitumen is
extracted by steam assisted gravity techniques. However it is to be understood
herein,
that the invention is applicable to the upgrading (i.e. the rendering better
or more easily
pumpable) of other similar or analogous types of hydrocarbon materials (e.g.
any
hydrocarbon material having an undesirable API from the stand point of pumping
such
as, for example, an API of 16 or less (e.g. an API of less than 12 e.g. of 8
to 12), e.g.
heavy oil).
Background
Supercritical water exists at temperatures and pressures above the critical
point of water
(of 221 bar and 374 C). The physical chemical properties of supercritical
water is
extensively described in Appendix I hereinafter (Supercritical Water oxidation
Technology, Tester et al), Relevant properties of supercritical water may be
summarised as follows.
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= Supercritical water has unique solvent properties in that hydrocarbons and
gasses are 100% solvable and inorganic (salts) are insoluble and will
precipitate out.
= When oxygen is dissolved in supercritical water and comes in contact with
organic material (i.e. hydrocarbon) it results in a spontaneous combustion.
This combustion is often termed SuperCritical Wet Oxidation (SCWO)
= Supercritical water has unique chemical properties in that it possesses a
certain reforming activity it can hydrolyse cellulose, it can act as a
reducing
agent (hydrogen donor) in hydrocarbon cracking and reforming.
There exists numerous references to processes for cracking, desulfurizing,
denitrifying,
demetalating, and generally upgrading hydrocarbon or coal fractions by
processes
involving supercritical water. As early as 1976 McCollum et al.(US-Patent
3,983,027)
described a supercritical water process for upgrading coal in absence of
hydrogen,
carbon monoxide or catalysts. Process patents have been filed covering various
aspects of
coal and bitumen recovery and upgrading by application of supercritical water.
The
specific application of supercritical water for upgrading bitumen is
extensively described
by Kamimura et al (Fuels for the Year 2000 and Beyond, Am. Chem. Soc Division
of
Fuel Chemistry, Boston, 1998) and by Berkowitz et al, (USPTO 20070056881).
Kamimura et al. has also filed a patent (CA 2,220,800) which specifically
addresses the
application of supercritical water to the SAGD-process.
The SuperCritical Wet Oxidation (SCWO) component of the present invention
exploits
(e.g. in a reactor) combustion of a portion of hydrocarbon (e.g. petroleum)
type material
to provide the energy needed for the upgrading, etc. thereof; i.e.
exploitation of the
supercritical conditions for a mixture of hydrocarbon material and water. It
is to be
understood herein that reference to" supercritical water oxidation component"
is a
reference to a component wherein the supercritical conditions are in relation
to a mixture
of hydrocarbon material and water.
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The present invention is in particular distinct from the respective Kammimura,
Berkowitz
and any other related processes in that energy recovery (and optionally carbon
capture)
may if desired or necessary comprise part of the bitumen recovery process of
the present
invention.
The invention may, for example, be directed to an upgrade method and/or system
which
may be used to upgrade the hydrocarbon content or moiety of a material such as
a hydrocarbon source component comprising a mixture of hydrocarbon
material (e.g. bitumen or any hydrocarbon material having an API of 16 or
less e.g. heavy oil) and water; the mixture may for example be at a pressure
P2 of less than or equal to 10 bar and a temperature of T2 of less than 180
C;
the mixture may for example comprise a water to oil mass ratio of 3:1 but
such ratio may for example be in the range of from 3:1 to (where possible)
1:1.
An upgrade method and/or system of the present invention may comprise
a) a pressurizing component (e.g. pump element) for subjecting a mixture
of hydrocarbon material (e.g. bitumen, heavy-oil, etc.) and water to a
predetermined pressure (e.g. P3) suitable for supercritical type water
oxidation (e.g. a pressure of 221 bar or higher; the temperature T3 of
the pressurised water and oil combination may for example be less
than about 180 C;
b) a supercritical water oxidation (e.g. reactor) component to which is fed
the obtained pressurised mixture of hydrocarbon material (e.g.
bitumen, heavy-oil, etc.) and water as well as an oxidising agent (e.g.
pure 02, hydrogen peroxide, air, etc. but pure 02 has the advantage
over air in that undesirable nitrogen by products may be avoided ) for
inducing combustion of a predetermined amount of bitumen (or heavy-
oil) material in order to raise the temperature of the hydrocarbon
material (e.g. bitumen, etc.)-water mixture to cracking temperature
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CA 02637421 2008-07-10
level (e.g. a temperature of from 372 C to 700 C or higher where
applicable), the conditions of pressure and temperature of the
hydrocarbon material (e.g. bitumen, etc.)-water feed being suitable for
supercritical water oxidation; e.g. the amount, pressure and
temperature of injected 02 may be controlled with a view to obtaining
the desired temperature conditions for cracking purposes due to such
in situ combustion (e.g. the oxygen feed pressure may be just
sufficient to be able to be injected into the bitumen-water mixture but
may as desired or necessary be higher); and
c) a cracking(/mineral separation) component configured to hold the
heated hydrocarbon material (e.g. bitumen)-water mixture (e.g. as a
function of temperature and pressure, if present also type of catalyst,
so as to provide a residence time which may vary from minutes to
seconds e.g. a residence time of fifteen minutes or less) for facilitating
the desired upgrading (i.e. upgrading meaning cracking to obtain a
cracked product having the desired pumpability characteristics e.g. an
API of 20 to 30) and, if desired, for example, mineral separation as
described herein.
In accordance with the present invention the pressurizing component,
supercritical water
oxidation component and the cracking (/mineral separation) component may be
individual components or may be combined with one or both of the other
components.
The invention may, for example, be directed to an upgrade method and/or system
which
may comprise a plurality of components. A system in accordance with the
present
invention may for example in particular comprise;
- a hydrocarbon source component comprising a mixture of hydrocarbon material
(e.g.
bitumen or any hydrocarbon material having an API of 16 or less e.g. heavy
oil) and
water; (e.g. at a pressure P2 of less than or equal to10 bar and a temperature
of T2 of less
than 180 C; e.g. at a water to oil mass ratio of 3:1 but such ratio may for
example be in
the range of from 3:1 to (where possible) 1:1;
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- a pressurizing component (e.g. pump element) for subjecting the hydrocarbon
material
(e.g. bitumen, heavy-oil, etc.) and water to a predetermined pressure (e.g.
P3) suitable
for supercritical type water oxidation (e.g. a pressure of 221 bar or higher;
the
temperature T3 of the pressurised water and oil combination may for example be
about
the same as T2 (see above);
- a supercritical water oxidation (e.g. reactor) component to which is fed the
obtained
pressurised mixture of hydrocarbon material (e.g. bitumen, heavy-oil, etc.)
and water as
well as an oxidising agent (e.g. pure 02, air, etc.) for inducing combustion
of a
predetermined amount of hydrocarbon material (e.g. bitumen, heavy-oil or the
like) in
order to raise the temperature of the bitumen-water mixture to cracking
temperature
level, the conditions of pressure and temperature of the bitumen-water feed
being
suitable for supercritical water oxidation; e.g. the amount, pressure and
temperature of
injected 02 may be controlled with a view to obtaining the desired temperature
conditions for cracking purposes due to such in situ combustion;
- a cracking(/mineral separation) component configured to hold the heated
mixture of
hydrocarbon material (e.g. bitumen, etc.) as a function of temperature and
pressure, if
present also type of catalyst, so as to provide a residence time which may
vary from
minutes to seconds e.g. a residence time of fifteen minutes or less) -water
mixture for
facilitating the desired upgrading (i.e. upgrading meaning cracking to obtain
a cracked
product having the desired pumpability characteristics e.g. an API of 20 to
30) and, for
example, mineral separation as described herein;
- a temperature reduction component for reducing the temperature of the
cracked product
for separation of the cracked product into a water phase and an organic phase;
e.g. reduce
to a temperature, for example, less than 372 C (e.g. from 300 to 372 C);
- a phase separation component for splitting the temperature reduced output
from the
cracking(/separation) component into water phase stream and an organic phase
stream
comprising a CO2 part and an oil part; the water phase stream may fior example
being
directed to the pressurizing) component to pass there through so as to reduce
its pressure
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CA 02637421 2008-07-10
for subsequent injection back into the in-ground reservoir component while
inducing
pressurisation of the extracted bitumen (or heavy-oil) and water as mentioned
above;
- an organic phase splitter component for splitting the organic phase into an
oil stream
(e.g. of API 20 to 30) and a COZ stream; and
- an optional CO2 capture component - or optionally the CO2 could be released
into the
atmosphere if traded for carbon credit.
The invention may in particular be exploited in conjunction with a steam
assisted gravity
drainage (SAGD), namely steam assisted gravity drainage (SAGD) component
comprising
a steam injection element for injecting steam at predetermined pressure and
temperature
(e.g. a pressure PI of less than 35 bar (e.g. up to 10 bar) and a temperature
Ti of less than
250 C (e.g. from 120 to 250 C; e.g. from 120 to 180 C) into the in-ground
bitumen (or
heavy oil) reservoir and a fluid extraction element for the extraction of
bitumen (or heavy-
oil) and water out of the reservoir (e.g. at a water to oil mass ratio of 3:1
but such ratio may
for example be in the range of from 3:1 to (where possible) 1:1; at a
temperature T2 < T,
(e.g. 100 to 200 ); at a pressure P2 < Pi( e.g. a pressure of 15 bar or
less)); the injection
and/or extraction may be assisted by pump elements but if desired the pressure
of the steam
injection may be arranged such the input steam pressure is not only sufficient
to inject
steam into the reservoir but also to force the water/oil mixture out of the
reservoir
Thus the invention may, for example, be directed to an upgrade method and/or
system for
upgrading bitumen (etc.) from an in ground reservoir which may comprise a
plurality of
additional components. A system in accordance with the present invention may
thus for
example comprise:
la) a hydrocarbon in-ground reservoir component comprising bitumen
or heavy oil (e.g. any hydrocarbon material having an API of 16 or less);
2a) a steam assisted gravity drainage (SAGD) component comprising a
steam injection element for injecting steam at predetermined pressure and
temperature (e.g. a pressure Pi of less than 35 bar (e.g. up to 10 bar) and a
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CA 02637421 2008-07-10
temperature Ti of less than 250 C (e.g. from 100 to 180 C) into the in-
ground bitumen (or heavy oil) reservoir and a fluid extraction element for the
extraction of bitumen (or heavy-oil) and water out of the reservoir (e.g. at a
water to oil mass ratio of 3:1 but such ratio may for example be in the range
of
from 3:1 to (where possible) 1:1; at a temperature Tz < Ti and a pressure P2 <
Pi); the injection and/or extraction may be assisted by pump elements but if
desired the pressure of the steam injection may be arranged such the input
steam pressure is not only sufficient to inject steam into the reservoir but
also
to force the water/oil mixture out of the reservoir;
3a) a pressurizing component (e.g. pump element) for subjecting the
extracted bitumen (or heavy-oil) and water to a predetermined pressure (e.g.
P3) suitable for supercritical water oxidation (e.g. a pressure of 221 bar or
higher; the temperature T3 of the pressurised water and oil combination may
for example be about the same as T2 (see above);
4a) a supercritical water oxidation (e.g. reactor) component to which is
fed the obtained pressurised bitumen (or heavy-oil) and water as well as an
oxidising agent (e.g. pure 02, air, etc.) for inducing combustion of a
predetermined amount of bitumen (or heavy-oil) material in order to raise the
temperature of the bitumen-water mixture to cracking temperature level, the
conditions of pressure and temperature of the bitumen-water feed being
suitable for supercritical water oxidation; e.g. the amount, pressure and
temperature of injected 02 may be controlled with a view to obtaining the
desired temperature conditions for cracking purposes due to such in situ
combustion;
5a) a cracking(/mineral separation) component configured to hold (e.g.
provide a residence time of fifteen minutes) for facilitating the desired
upgrading (i.e. upgrading meaning cracking to obtain a cracked product
having the desired pumpability characteristics e.g. an API of 20 to 30) and,
for
example, mineral separation as described herein;
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6a) a temperature reduction component for reducing the temperature
of the cracked product for separation of the cracked product into a water
phase
and an organic phase; e.g. reduce to a temperature, for example, less than
372 C (e.g. from 300 to 372 C);
7a) a phase separation component for splitting the temperature reduced
output from the cracking(/separation) component into water phase stream and
an organic phase stream comprising a CO2 part and an oil part; the water
phase stream may for example being directed to the pressurizing) component
to pass there through so as to reduce its pressure for subsequent injection
back
into the in-ground reservoir component while inducing pressurisation of the
extracted bitumen (or heavy-oil) and water as mentioned above;
8a) an organic phase splitter component for splitting the organic phase
into an oil stream (e.g. of API 20 to 30) and a CO2 stream;
9a) an optional COZ capture component - or optionally the CO2 could
be released into the atmosphere if traded for carbon credit.
If desired the pressurizing component and the supercritical water oxidation
component
may be combined into a more or less single component.
The invention is directed to a method and/or system which may be run
continuously; run
by batch; or run semi batch wise. The method and\or system may, for example,
be run as
a closed or open loop for the extraction of bitumen from a bitumen reservoir.
The system can be run in batch or in continuous operation:
= Batch:
o The system may be fed at the proper pressure (i.e. more than 221
bar or) in the range of necessary pressure to eventually reach the
vapour-liquid region indicative of conditions under which water has
the properties of supercritical water until the reactor is full. Then the
02 is injected to increases the temperature needed to get the
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CA 02637421 2008-07-10
supercritical water properties required for cracking. The fluids stay
in the reactor until the cracking of heavy oil/bitumen is cracked to
an API of 20 to 30 under the specific condition of the super critical
water properties and until the precipitation of the minerals settling
down to the bottom of the vessel is completed. Then the vessel is
emptied into an oil and water separator to create a stream of Water
and a stream of oil and dissolved C02.
= Continuous
o The same process is applied at the exemption that the reactor is
design to have a constant and uniform flow that produce a sufficient
residence time to properly achieved the cracking of the heavy
oil/bitumen as well as the separation of the precipitate mineral to
the bottom of the reactor.
In any event residence time for cracking is that needed to obtain the desired
upgraded
API number (e.g. 20 to 30)
As may be appreciated the present invention may exploit or incorporate aspects
of the
following:
1. Super-Critical-Water-Oxidation (SCWO) process (see Appendix 1)
2. SAGD (Steam Assisted Gravity Drainage) process for bitumen recovery (see
Appendix 2: Study on New Upgrading Process of Heavy Oils Combined with
SAGD by means of Hydrothermal Treatment, Kishita et al)
3. Super-Critical-Water (SCW)-reforming and upgrading (see Appendix 2)
4. Supercritical steam turbines for power generation (available from Siemens
or GE)
The SCWO based process (i.e. method - system) of the present invention may for
example comprises a closed loop, as illustrated in Fig.la (just below), where
live steam is
injected into the bituminous formation (1) to facilitate mobilisation of the
bitumen by
gravity drainage and recovering at the surface as a hot bitumen-water (2)
emulsion
(SAGD). Said emulsion is pressurized to minimum 221 bar (3), fed into a Super-
Critical-
CA 02637421 2008-07-10
Wet-Oxidation (SCWO) reactor (4), and heated to minimum 374 C by direct
injection of
oxygen (5) which facilitates spontaneous stoiciometric combustion of a
representative
fraction of the bitumen in place. The reaction product comprises now three
components,
water, bitumen and C02, which exists in one homogeneous phase. The product is
held at
a specified pressure and temperature (exceeding the critical point of the
hydrocarbon/water mixture) in a vessel (6) for the required time to facilitate
the required
upgrading (i.e. cracking) and demineralization (7) of the bitumen. Cold makeup
water is
added (10) The product is then further cooled (8) and/or depressurised (9) to
below the
critical point of the hydrocarbon/water mixture to facilitate a phase
separation of water
from the contentious oil/COZ-phase (11). Energy is recovered as the water
phase is
expanded over a steam turbine (12) down to the required pressure and
temperature for
live steam injection (1) into the bituminous formation. The homogeneous
Oil/CO2 is
cooled and depressurised (14) to below the critical point of CO2 (72 bar 31 C)
to separate
CO2 from oil. COz is captured for deposit in the ground and oil goes to
export.
'{i 5 1p, On Sife Bitumen Recovery, Upgrading, Carbon Capture & Storage
C02
St ge Water makeup
10 6 T>372 C
T<3tC
P`=2 13 Separator U_ SCwo 02 e s s p
1~ . T<372 C 4
.e~_.i.=_=,a grad
PZ221~9-
water LJ9
minerals P>221bar
. ~ - . - . - . - . - . - . - . - . - . - . - . - . - . 3
T=235 C I1 T=i80C
2 P=8 bar
. . . P=30 bar
. ... . .rv.... . . . rsw.aar...
VvYax.a., r~[a[tcxrvr~
W<ai
Advantages of the present invention as compared to the standard SAGD process.
1. No independent diluents needed; make pumpable hydrocarbon fluid without the
specific addition of a diluent(s);
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CA 02637421 2008-07-10
2. On Site Upgrading (i.e. cracking);
3. No boiler or Steam generator may be needed; may use heated water from
cracking to produce steam for injection into a hydrocarbon reservoir;
4. No water treatment may be needed; i.e. water from cracking may go directly
to
injection;
5. Oil Product may be demineralised (Sulphur and heavy metals removed by
precipitation)
6. C02 may be captured & deposited and/or can be traded for carbon credits.
Stated otherwise the present invention provides a Method for on site bitumen
recovering, upgrading and if desired carbon-capture by
= Pressurise the bitumen/water emulsion from the SAGD process to a pressure
above 221 bar.
= Heat said emulsion to a specific temperature e.g. above 377 C by injection
of
adequate amount of oxygen into a scwo reactor such that a single "liquid"
phase is
formed. i.e. what structural (mechanical parts, etc.) as well as operational
details
= Hold the "liquid" for a certain time to allow for completion of the
reforming/upgrading process (i.e. cracking) and to allow for the
precipitation/settling of inorganic components
= Remove the precipitates
= Bring the said "liquid" into sub-critical-state by dropping pressure and or
temperature to below the critical point such that a two-phase region is
formed,
comprising an lower aqueous phase and an upper hydrocarbon-CO2 phase.
= Recover energy by expanding the lower aqueous phase over a steam turbine
down
to the required pressure and temperature for steam injection in the SAGD
process.
= Cool and/or depressurise the upper phase to below its critical point to
facilitate
flashing of CO2.
= Optionally Recover C02 for under ground storage/deposit.
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Stated otherwise the present invention also provides a system for on site
bitumen
recovery, and upgrading (and if desired or necessary carbon-capture)
comprising:
= Pressurise the bitumen/water emulsion from the SAGD process to a pressure
above 221 bar.
= Heat said emulsion to a specific temperature above 377 C by injection of
adequate amount of oxygen into a swoc reactor such that a single "liquid"
phase is
formed.
= Hold the "liquid" for a certain time to allow for completion of the
reforming/upgrading process and to allow for the precipitation/settling of
inorganic components.
= Remove the precipitates
= Bring the said "liquid" into sub-critical-state by dropping pressure and or
temperature to below the critical point such that a two-phase region is
formed,
comprising an lower aqueous phase and an upper hydrocarbon-CO2 phase.
= Recover energy by expanding the lower aqueous phase over a steam turbine
down
to the required pressure and temperature for steam injection in the SAGD
process.
= Cool and/or depressurise the upper phase to below its critical point to
facilitate
flashing of COZ.
= Optionally if desired or necessary Recover CO2 for under ground
storage/deposit
= If desired or necessary, a cracking aid material such KOH, NaOH, CO, H2
and/or
cracking catalyst(s) may be exploited in the cracking step - if a cracking
catalyst
is exploited cracking may be accomplished after precipitate separation (e.g.
to
avoid catalyst poisoning).
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CA 02637421 2008-07-10
In accordance with a further example aspect of the present invention there is
provided a
recovery technology which may comprise a closed loop, as illustrated in
Fig.2a, where
live steam is injected into the bituminous formation (1 A) to facilitate
mobilisation of the
bitumen by gravity drainage and recovering at the surface as a hot bitumen-
water (2A)
emulsion (SAGD). Said emulsion is pressurized to minimum 221 bar (3A), heated
in a
heat exchanger (4A) and fed into a vessel (6A) and further heated to the
required
temperature by being mixed with a hot stream exiting from a Super-Critical-Wet-
Oxidation (SCWO) reactor (8A). The energy output from a SCWO-reactor is
dictated
by the hydrocarbon injection rate (13A) and the temperature is controlled by
the water
rate (12A + 15A). A spontaneous combustion of the hydrocarbons results when a
stoiciometric excess, for example, of from 1 to 10% oxygen is injected (14a)
into the
SCWO-reactor. When excess oxygen is injected, the combustion is normally
complete,
yielding only C02 and water.
The reaction product comprises now three components, water, bitumen and C02,
which
exists in one homogeneous phase. The product is held at a specified pressure
and
temperature (exceeding the critical point of water) in the vessel (6A) for the
required
time to facilitate the required upgrading and demineralization of the bitumen.
The higher
the temperature and pressure the lower the time required for upgrading. To
achive less
than one minute holding time for completion, high temperature and pressure is
desired,
but this is normally compromised by limitations in material properties of the
vessels and
piping. Minerals will precipitate and are removed by filter (7A). The product
is then
cooled by the feed stream in the heat exchanger (4A ) to below the critical
point of water
to facilitate a phase separation of water from the contentious oil/COZ-phase
(9A).
Energy is recovered as the water phase is expanded over a Steam-or Pelton-
turbine
(l0A) down to the required pressure and temperature for live steam injection
(1A) into
the bituminous formation. The homogeneous Oil/CO2 is cooled (15A) and
depressurised
(16A) to below its critical point to separate C02 from oil. COz is de-oiled in
a scrubber
(17A) and captured for deposit in the ground and oil goes to export (18A) .
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Alterative features with respect to oxygen insertion to increase temperature:
o A) Using a reactor were the fluid is fed and uniformly mixed with
the proper ratio of oxygen to increase the temperature to the super
critical envelop. The residence time and the flow of Oxygen are
variable that control the final temperature. (see figure 3a)
o Using a pipe were the fluid is fed and uniformly mixed with the
proper ratio of oxygen to increase the temperature to the super
critical envelop. The residence time and the flow of Oxygen are
variable that control the final temperature. (see figure 4a)
o Using a stream flow were the fluid is fed and uniformly mixed with
the proper ratio of oxygen to increase the temperature to a higher
then desired final temperature. The residence time and the flow of
Oxygen are variable that control the final temperature the stream
flow is then blend back with the main stream to obtain the final
temperature witch is in the supercritical envelop. (see figure 5a);
and
o Using the pump as a mixing chamber to inject the 02 and the pipe
or a reactor to generate the proper residence time for the reaction.
(see figure 6a);.
Cracking of heavy hydrocarbon materials is known. Upgrading or cracking as
referred to
herein is to be understood as relating to a process whereby process conditions
such as
pressure, temperature etc. are set so as to allow for the production of
smaller molecular
weight materials from materials of higher molecular weight rendering the final
product
mixture relatively more easily pumped than the initial starting material.,
i.e. the cracking
may result in the production of materials which may in effect function as
diluents for the
remaining bitumen material - in any event no matter what the mechanism which
raises
the API number the purpose of the cracking is to achieve a product that is
relatively
pumpable.
CA 02637421 2008-07-10
Mineral separation may also be achieved during the supercritical condition,
i.e. when the
pressure and temperature are kept in the supercritical water envelop, the
Water and the
hydrocarbon become one phase and the mineral are precipitating and separated
by
gravity. It is then possible to collect at the bottom of the vessel Salt,
Coke, Vanadium,
heavy metal, sulphur etc..
For phase separation the temperature and pressure are decreased just under the
Supercritical water envelop to initiate the phase separation between the Water
and the
organic phase including the CO2. Under the supercritical point water and
organic phase
become again two distinct phase. Because the density between the Water and the
oil is
substantial the separation is easier than the traditional water bitumen
separation.
^ The temperature is less than 372 C
^ The pressure is less than 221 bar
Carbon dioxide storage may be achieved by any known storage technique for this
purpose - e.g. geological storage by be used whereby the carbon dioxide may be
shipped
by pipeline to a suitable geological storage site and injected into a suitable
geological
formation underground in any (known ) manner.
16
