Patent Application
20060207762
This invention relates to a process for improved safety and productivity when undertaking oil recovery from an underground reservoir by the toe-to-heel in situ combustion process employing horizontal production wells, such as disclosed in U.S. Pat. Nos. 5,626,191 and 6,412,557. More particularly, it relates to an in situ combustion process in which a water, steam, and/or a non-oxidizing gas which in a preferred embodiment is carbon dioxide which acts as a gaseous solvent, is injected into the reservoir for improving recovery in an in situ combustion recovery process.
U.S. Pat. Nos. 5,626,191 and 6,412,557, incorporated herein in their entirety, disclose in situ combustion processes for producing oil from an underground reservoir (100) utilizing an injection well (102) placed relatively high in an oil reservoir (100) and a production well (103-106) completed relatively low in the reservoir (100). The production well has a horizontal leg (107) oriented generally perpendicularly to a generally linear and laterally extending upright combustion front propagated from the injection well (102). The leg (107) is positioned in the path of the advancing combustion front. Air, or other oxidizing gas, such as oxygen-enriched air, is injected through wells 102, which may be vertical wells, horizontal wells or combinations of such wells. The process of U.S. Pat. No. 5,626,191 is called “THAI™”, an acronym for “toe-to-heel air injection” and the process of U.S. Pat. No. 6,412,557 is called “Capri™”, the Trademarks being held by Archon Technologies Ltd., a subsidiary of Petrobank Energy and Resources Ltd., Calgary, Alberta, Canada.
High-Pressure-Air-Injection, HPAI, is an in situ combustion process that is applied in tight reservoirs containing light oil. In these reservoirs, a liquid such as water cannot be effectively injected because of low reservoir permeability. Air is injected in the upper reaches of the reservoir and oil drains into a horizontal well placed low in the reservoir. The process provides some heat by low-temperature oil oxidation and more importantly, it provides pressure-maintenance to enable high sustained oil rates. This process can be applied in any reservoir that contains oil that is mobile at reservoir conditions. Of concern is the safety of the THAI™ and Capri™ processes with respect to oxygen entry into the horizontal well, which would cause oil burning in the well and extremely high temperatures that would destroy the well. Such oxygen breakthrough will not occur if the injection rates are kept low, however, high injection rates are very desirable in order to maintain high oil production rates and a high oxygen flux at the combustion front. A high oxygen flux is known to keep the combustion in the high-temperature oxidation (HTO) mode, achieving temperatures of greater than 350° C. and combusting the fuel substantially to carbon dioxide. At low oxygen flux, low-temperature oxidation (LTO) occurs and temperatures do not exceed ca. 350° C. In the LTO mode, oxygen becomes incorporated into the organic molecules, forming polar compounds that stabilize detrimental water-oil emulsions and accelerate corrosion because of the formation of carboxylic acids. In conclusion, the use of relatively low oxidant injection rates is not an acceptable method to prevent combustion in the horizontal wellbore.
What is needed is one or more methods to increase the oxidizing gas injection rate while preventing oxygen entry into the horizontal wellbore. The present invention provides such methods.
The THAI™ and Capri™ processes depend upon two forces to move oil, water and combustion gases into the horizontal wellbore for conveyance to the surface. These are gravity drainage and pressure. The liquids, mainly oil, drain into the wellbore under the force of gravity since the wellbore is placed in the lower region of the reservoir. Both the liquids and gases flow downward into the horizontal wellbore under the pressure gradient that is established between the reservoir and the wellbore.
During the reservoir pre-heating phase, or start-up procedure, steam is circulated in the horizontal well through a tube that extends to the toe of the well. The steam flows back to the surface through the annular space of the casing. This procedure is imperative in bitumen reservoirs because cold oil that may enter the well will be very viscous and will flow poorly, possible plugging the wellbore. Steam is also circulated through the injector well and is also injected into the reservoir in the region between the injector wells and the toe of the horizontal wells to warm the oil and increase its mobility prior to initiating injection of oxidizing gas into the reservoir.
The aforementioned Patents show that with continuous oxidizing gas injection a quasi-vertical combustion front develops and moves laterally from the direction of the toe of the horizontal well towards the heel. Thus two regions of the reservoir are developed relative to the position of the combustion zone. Towards the direction of toe, lies the oil-depleted region that is filled substantially with oxidizing gas, and on the other side lies the region of the reservoir containing cold oil or bitumen. At higher oxidant injection rates, reservoir pressure increases and the fuel deposition rate can be exceeded, so that gas containing residual oxygen can be forced into the horizontal wellbore in the oil-depleted region.
The consequence of having oil and oxygen together in a wellbore is combustion and potentially an explosion with the attainment of high temperatures, perhaps in excess of 1000° C. This can cause irreparable damage to the wellbore, including the failure of the sand retention screens. The presence of oxygen and wellbore temperatures over 425° C. must be avoided for safe and continuous oil production operations.
Several methods of preventing oxygen entry into the producing wellbore are based on reducing the differential pressure between the reservoir and the horizontal wellbore. These are 1. to reduce the injection rate of the oxidizing gas in order to reduce the reservoir pressure, and 2. to reduce the fluid drawdown rate to increase wellbore pressure. Both of these methods result in the reduction of oil rates, which is economically detrimental. Conventional thinking would also state that injecting fluid directly into the wellbore would increase wellbore pressure but would be very detrimental to production rates.
Importantly, it has been discovered that in an in situ combustion process generally, if carbon dioxide is injected into the reservoir along with the oxidizing gas, the oil recovery rate is increased. This is true whether the ISC process is of the traditional, THAI™, Capri™, HPAI or any other type.
Specifically, when the injected non-oxidizing gas which is injected with oxygen comprises only carbon dioxide in the absence of nitrogen, the improvement can be dramatic.
Thus in a preferred embodiment of the invention, the injected non-oxidizing gas is carbon dioxide.
Advantageously, in an in situ combustion recovery process, when O2 is injected alone, the recovered combustion gas, which substantially comprises CO2, can be compressed and mixed with the oxygen. Any ratio of O2 to CO2 can be attained by adjusting the percentage of recycled produced CO2.
If the produced combustion gas contains impurities, these will not build-up if an appropriate slip stream of combustion gas is disposed.
Since the disposed gas will be typically about 95% CO2 it can be sold without purification for enhanced oil recovery by miscible flooding, or can be disposed into a deep aquifer.
It is not required that the CO2 be miscible (ie. soluble in all proportions) in the oil under reservoir conditions. Partial solubility is adequate.
While the mechanics of how adding a particular non-oxidizing gas such as CO2, as opposed to other non-oxidizing gases, further increases the mobility of hydrocarbons in a reservoir are not precisely understood, and without being in any way held to an explanation as to why such important increases in recoverability are obtained as a result of CO2 injection, it is suspected that CO2 acts as a solvent and decreases the oil viscosity ahead of the combustion zone, thereby enhancing the combustion process and thus further liquefying oil ahead of the combustion zone. The added dissolution of some CO2 in the combustion front also facilitates the transfer of heat from the combustion gas into the oil, which also reduces the oil viscosity, thus increasing recovery.
Thus in order to overcome the disadvantages of the prior art, and to improve the safety or productivity of hydrocarbon recovery from an underground reservoir, the present invention accordingly in a first broad embodiment comprises a process for extracting liquid hydrocarbons from an underground reservoir comprising the steps of:
In a further broad embodiment of the invention, the present invention comprises a process for extracting liquid hydrocarbons from an underground reservoir, comprising the steps of:
In a still further embodiment of the invention, the present comprises the combination of the above steps of injecting a medium to the formation via the injection well, and as well injecting a medium via tubing in the horizontal leg. Accordingly, in this further embodiment the present invention comprises a method for extracting liquid hydrocarbons from an underground reservoir, comprising the steps of:
If the medium is steam, it is injected into the reservoir/formation, via either or both the injection well or the production well via tubing therein, in this state, typically under a pressure of 7000 KpA.
Alternatively, where the injected medium is water, such method contemplates that the water become heated at the time of supply to the reservoir to become steam. The water, when it reaches the formation, via either or both the injection well and/or the tubing in the production well, may be heated to steam during such travel, or immediately upon its exiting of the injection well and/or tubing in the production well and its entry into the formation.
Lastly, in a further broad aspect of the present invention for use in an in-situ combustion hydrocarbon recovery process from subterranean deposits, the method of the present invention comprises the steps of:
(a) providing at least one injection well for injecting an oxidizing gas into an upper part of an underground reservoir;
(b) said at least one injection well further adapted for injecting carbon dioxide into a lower part of an underground reservoir;
(c) providing at least one production well;
(d) injecting an oxidizing gas through the injection well for in situ combustion, so that combustion gases are produced;
(e) injecting carbon dioxide alone or in combination with oxyen into said injection well; and
(f) recovering hydrocarbons from said production well.
In another variation of the above, the method of the present invention comprises a process for extracting liquid hydrocarbons from an underground reservoir, comprising the steps of:
(a) providing at least one oxidizing gas injection well for injecting an oxidizing gas into an upper part of an underground reservoir;
(b) providing at least one other injection well for injecting carbon dioxide into a lower part of an underground reservoir;
(c) providing at least one production well;
(d) injecting an oxidizing gas through the oxidizing injection well for in situ combustion, so that combustion gases are produced,;
(e) injecting carbon dioxide alone or in combination with oxyen into said other injection well ; and
(f) recovering hydrocarbons from said production well.
It is to be noted that, where CO2 is injected into the injection well, one or more additional non-oxidizing gasses could also be injected at the same time in combination with the CO2.
Item A represents the top level of a heavy oil or bitumen reservoir, and B represents the bottom level of such reservoir/formation.
C represents a vertical well with D showing the general injection point of a oxidizing gas such as air.
E represents a general location for the injection of steam or a non-oxidizing gas into the reservoir. This is part of the present invention.
F represents a partially perforated horizontal well casing. Fluids enter the casing and are typically conveyed directly to the surface by natural gas lift through another tubing located at the heel of the horizontal well (not shown).
G represents a tubing placed inside the horizontal leg. The open end of the tubing may be located near the end of the casing, as represented, or elsewhere. The tubing can be ‘coiled tubing’ that may be easily relocated inside the casing. This is part of the present invention.
The elements E and G are part of the present invention and steam or non-oxidizing gas may be injected at E and/or at G. E may be part of a separate well or may be part of the same well used to inject the oxidizing gas. These injection wells may be vertical, slanted or horizontal wells or otherwise and each may serve several horizontal wells.
For example, using an array of parallel horizontal leg as described in U.S. Pat. Nos. 5,626,191 and 6,412,557, the steam, water or non-oxidizing gas may be injected at any position between the horizontal legs in the vicinity of the toe of the horizontal legs.
length A-E is 250 m; width A-F is 25 m; height F-G is 20 m.
The positions of the wells are as follows:
Oxidizing gas injection well J is placed at B in the first grid block 50 meters (A-B) from a comer A. The toe of the horizontal well K is in the first grid block between A and F and is 15 m (B-C) offset along the reservoir length from the injector well J. The heel of the horizontal well K lies at D and is 50 m from the corner of the reservoir, E. The horizontal section of the horizontal well K is 135 m (C-D) in length and is placed 2.5 m above the base of the reservoir (A-E) in the third grid block.
The Injector well J is perforated in two (2) locations. The perforations at H are injection points for oxidizing gas, while the perforations at I are injection points for steam or non-oxidizing gas. The horizontal leg (C-D) is perforated 50% and contains tubing open near the toe (not shown, see
The operation of the THAI™ process has been described in U.S. Pat. Nos. 5,626,191 and 6,412,557 and will be briefly reviewed. The oxidizing gas, typically air, oxygen or oxygen-enriched air, is injected into the upper part of the reservoir. Coke that was previously laid down consumes the oxygen so that only oxygen-free gases contact the oil ahead of the coke zone. Combustion gas temperatures of typically 600° C. and as high as 1000° C. are achieved from the high-temperature oxidation of the coke fuel. In the Mobile Oil Zone (MOZ), these hot gases and steam heat the oil to over 400° C., partially cracking the oil, vaporizing some components and greatly reducing the oil viscosity. The heaviest components of the oil, such as asphaltenes, remain on the rock and will constitute the coke fuel later when the burning front arrives at that location. In the MOZ, gases and oil drain downward into the horizontal well, drawn by gravity and by the low- pressure sink of the well. The coke and MOZ zones move laterally from the direction from the toe towards the heel of the horizontal well. The section behind the combustion front is labeled the Burned Region. Ahead of the MOZ is cold oil.
With the advancement of the combustion front, the Burned Zone of the reservoir is depleted of liquids (oil and water) and is filled with oxidizing gas. The section of the horizontal well opposite this Burned Zone is in jeopardy of receiving oxygen which will combust the oil present inside the well and create extremely high wellbore temperatures that would damage the steel casing and especially the sand screens that are used to permit the entry of fluids but exclude sand. If the sand screens fail, unconsolidated reservoir sand will enter the wellbore and necessitate shutting in the well for cleaning-out and remediation with cement plugs. This operation is very difficult and dangerous since the Wellbore can contain explosive levels of oil and oxygen.
In order to quantify the effect of fluid injection into the horizontal wellbore, a number of computer numerical simulations of the process were conducted. Steam was injected at a variety of rates into the horizontal well by two methods: 1. via tubing placed inside the horizontal well, and 2. via a separate well extending near the base of the reservoir in the vicinity of the toe of the horizontal well. Both of these methods reduced the prediliction of oxygen to enter the wellbore but gave surprising and counterintuitive benefits: the oil recovery factor increased and build-up of coke in the wellbore decreased. Consequently, higher oxidizing gas injection rates could be used while maintaining safe operation.
It was found that both methods of adding steam to the reservoir provided advantages regarding the safety of the THAI™ Process by reducing the tendency of oxygen to enter the horizontal wellbore. It also enabled higher oxidizing gas injection rates into the reservoir, and higher oil recovery.
Extensive computer simulation of the THAI™ Process was undertaken to evaluate the consequences of reducing the pressure in the horizontal wellbore by injecting steam or non-oxidizing gas. The software was the STARS™ In Situ Combustion Simulator provided by the Computer Modelling Group, Calgary, Alberta, Canada.
Table 4. List of Model Parameters.
Simulator: STARS™ 2003.13, Computer Modelling Group Limited
Model dimensions:
Length 250 m, 100 grid blocks, eac
Width 25 m, 20 grid blocks
Height 20 m, 20 grid blocks
Grid Block dimensions: 2.5 m×2.5 m×1.0 m (LWH).
Horizontal Production Well:
A discrete well with a 135 m horizontal section extending from grid block 26,1, 3 to 80,1,3
The toe is offset by 15 m from the vertical air injector.
Vertical Injection Well:
Oxidizing gas(air) injection points: 20,1, 1:4 (upper 4-grid blocks)
Oxidizing gas injection rates: 65,000 m3/d, 85,000 m3/d or 100,000 m3/d
Steam injection points: 20, 1, 19:20 (lower 2-grid blocks)
Rock/Fluid Parameters:
Components: water, bitumen, upgrade, methane, CO2, CO/N2, oxygen, coke
Heterogeneity: Homogeneous sand.
Permeability: 6.7 D (h), 3.4 D (v)
Porosity: 33%
Saturations: Bitumen 80%, water 20%, gas Mole fraction 0.114
Bitumen viscosity: 340,000 cP at 10° C.
Bitumen average molecular weight: 550 AMU
Upgrade viscosity: 664 cP at 10° C.
Upgrade average molecular weight: 330 AMU
Physical Conditions:
Reservoir temperature: 20° C.
Native reservoir pressure: 2600 kPa.
Bottomhole pressure: 4000 kPa.
Reactions:
1. 1.0 Bitumen→0.42 Upgrade+1.3375 CH4+20 Coke
2. 1.0 Bitumen+16 O2ˆ0.05→12.5 water+5.0 CH4+9.5 CO2+0.5 CO/N2+15 Coke
3. 1.0 Coke+1.225 O2→0.5 water+0.95 CO2+0.05 CO/N2
Table 1a shows the simulation results for an air injection rate of 65,000 m3/day (standard temperature and pressure) into a vertical injector (E in
However, as may be seen from the data below, injection of low levels of steam at levels of 5 and 10 m3/day (water equivalent) at a point low in the reservoir (E in
*Not part of the present invention.
Table 1b shows the results of injecting steam into the horizontal well via the internal tubing, G, in the vicinity of the toe while simultaneously injecting air at 65,000 m3/day (standard temperature and pressure) into the upper part of the reservoir. The maximum wellbore temperature is reduced in relative proportion to the amount of steam injected and the oil recovery factor is increased relative to the base case of zero steam. Additionally, the maximum volume percent of coke deposited in the wellbore decreases with increasing amounts of injected steam. This is beneficial since pressure drop in the wellbore will be lower and fluids will flow more easily for the same pressure drop in comparison to wells without steam injection at the toe of the horizontal well.
*Not part of the present invention.
In this example, the air injection rate was increased to 85,000 m3/day (standard temperature and pressure) and resulted in oxygen breakthrough as shown in Table 2a. An 8.8% oxygen concentration was indicated in the wellbore for the base case of zero steam injection. Maximum wellbore temperature reached 1074° C. and coke was deposited decreasing wellbore permeability by 97%. Operating with the simultaneous injection of 12 m3/day (water equivalent) of steam at the base of the reservoir via vertical injection well C (see
*Not part of the present invention.
Table 2b shows the combustion performance with 85,000 m3/day air (standard temperature and pressure) and simultaneous injection of steam into the wellbore via an internal tubing G (see
*Not part of the present invention.
In order to further test the effects of high air injection rates, several runs were conducted with 100,000 m3/day air injection. Results in Table 3a indicate that with simultaneous steam injection at the base of the reservoir (ie at location B-E in vertical well C-ref.
*Not part of the present invention.
Table 3b shows the consequence of injecting steam into the well tubing G (ref.
*Not part of the present invention.
Table 4 below shows comparisons between injecting oxygen and a combination of non-oxidizing gases, namely nitrogen and carbon dioxide, into a single vertical injection well in combination with a horizontal production well in the THAI™ process via which the oil is produced, as obtained by the STARS™ In Situ Combustion Simulator software provided by the Computer Modelling Group, Calgary, Alberta, Canada. The computer model used for this example was identical to that employed for the above six examples, with the exception that the modeled reservoir was 100 meters wide and 500 meters long. Steam was added at a rate of 10 m3/day via the tubing in the horizontal section of the production well for all runs.
As may be seen from above Table 4 comparing Run 1 and Run 2, when the oxygen and inert gas are reduced by 50% as in Run2, the oil recovery is nevertheless the same as in Run 1, providing that the inert gas is CO2. This means that the gas compression costs are cut in half in Run 2, while oil is produced faster.
As may further be seen from above Table 4, Run #1 having 17.85 molar % of oxygen and 67.15% nitrogen injected into the injection well, estimated oil recovery rate was 41 m3/day. In comparison, using a similar 17.85 molar % oxygen injection with 67.15 molar % carbon dioxide as used in Run #4, a 3.3 times increase in oil production (136 m3/day) is estimated as being achieved.
As may be further seen from Table 4 above, when equal amounts of oxygen and CO2 are injected as in Run 6, still with a total injected volume of 85,000 m3/day, oil recovery was increased 2.7-fold.
Run 7 shows the benefit of adding CO2 to air as the injectant gas. Compared with Run 1, oil recovery was increased 1.7-fold without increasing compression costs. The benefit of this option is that oxygen separation equipment is not needed.
Referring now to
For a fixed amount of steam injection, the average daily oil recovery rate increased with air injection rate. This is not unexpected since the volume of the sweeping fluid is increased. However, it is surprising that the total oil recovered decreases as air rate is increased. This is during the life of the air injection period ( time for the combustion front to reach the heel of the horizontal well). Moreover, with carbon dioxide injected in the vertical well, and/or in the horizontal production well, production rates improved production rates can be expected.
Although the disclosure described and illustrates preferred embodiments of the invention, it is to be understood that the invention is not limited to these particular embodiments. Many variations and modifications will now occur to those skilled in the art. For definition of the invention, reference is to be made to the appended claims.
This application is a continuation-in-part of PCT application PCT/CA2005/000883 filed on Jun. 6, 2005 in which the United States was designated, claiming priority from U.S. Provisional Application 60/577,779 filed Jun. 7, 2004, each of which are incorporated herein by reference in their entirety and for all their teachings, disclosures and purposes.
| Number | Date | Country | |
|---|---|---|---|
| Parent | PCT/CA05/00883 | Jun 2004 | US |
| Child | 11364112 | Feb 2006 | US |
