Patent Application
20130206399
The invention is related to oil and gas industry and could be applicable to various thermal methods of heavy oil recovery in particular to the Steam Assisted Gravity Drainage (SAGD), huff and puff, cyclic steam injection, etc.
Heavy oil and bitumen account for more than double the resources of conventional oil in the world. Recovery of heavy oil and bitumen is a complex process requiring products and services built for specific conditions, because these fluids are extremely viscous at reservoir conditions (up to 1500000 cp). Heavy oil and bitumen viscosity decreases significantly with temperature increases and thermal recovery methods seems to be the most promising ones. Steam Assisted Gravity Drainage (SAGD) offers a number of advantages in comparison with other thermal recovery methods. Typical implementation of this method requires at least one pair of parallel horizontal wells drilled near the bottom of the reservoir one above the other. The upper well, “injector,” is used for steam injection, the lower well, “producer,” is used for production of the oil. SAGD provides greater production rates, better reservoir recoveries, and reduced water treating costs and dramatic reductions in Steam to Oil Ratio (SOR).
One of main problems of thermal recovery methods is the processes start-up. Due to high viscosity the cold oil is essentially immobile and therefore initial reservoir heating is required. This initial preheating stage is necessary to create a uniform thermo-hydraulic communication between the well pair, or create a heated zone around the well in the case of single well completion. During this start-up period, steam circulated in well(-s) to heat the reservoir and no (or little) oil production is assumed. This stage requires a lot of energy to be injected into the reservoir with the steam. Preheating stage strategy aims at minimizing the time in which well(-s) can be converted to the oil production operation regime as well as minimization of the amount of steam needed for circulation.
Thermal methods of heavy oil recovery are described in U.S. Pat. No. 4,085,803, published Apr. 25, 1978, U.S. Pat. No. 4,099,570 published Jul. 11, 1978 and in U.S. Pat. No. 4,116,275 published Sep. 26, 1978. Description of the SAGD process and its modifications is given in U.S. Pat. No. 4,344,485 published Aug. 17, 1982.
U.S. Pat. No. 6,988,549 published Jan. 24, 2006 discusses certain problems associated with typical SAGD projects. According to this patent the economics of such projects is significantly impacted by the cost associated with steam generation and SAGD does not typically employ the use of super-saturated steam because of the high cost of producing this steam with conventional hydrocarbon-fired tube boilers which results in using steam that is less efficient in transferring heat to the heavy oil reservoir.
The economics of SAGD may have been adversely affected by the duration of the preheating stage and the circulation steam rates at this stage. Commercial simulator numerical models were used to estimate SAGD preheating parameters (steam circulation rate and preheating stage duration). In particular: Vanegas Prada J. W., Cunha L. B., Alhanati F. J. S.: “Impact of Operational Parameters and Reservoir Variables During the Startup Phase of a SAGD Process,” SPE paper 97918; Vincent K. D., MacKinnon C. J., Palmgren C. T. S.: “Developing SAGD Operating Strategy using a Coupled Wellbore Thermal Reservoir Simulator,” SPE paper 86970; Shin H., Polikar M.: “Optimizing the SAGD Process in Three Major Canadian Oil-Sands Areas,” SPE paper 95754.
Nevertheless these models cannot be used for the fast estimation of the optimal preheating parameters for a wide range of reservoir properties and do not consider necessary changes of the well operating regimes at various time intervals of the preheating stage.
U.S. Pat. No. 5,215,146 published Jul. 1, 1993 describes one of the realizations of preheating process. Method given in this patent can reduce the duration of the preheating stage. In the described process steam is circulated in both horizontal wells with the constant considerable temperature gradient in-between them, which forces the heated fluids to move from upper to lower well. Certain amount of foam is injected in order to increase pressure gradient between the wells and hence the oil phase velocities. Increased oil rates will decrease preheating time but only after the time moment when thermo-hydraulic communication between well pair was achieved. This method is energy- and capital-expensive, as foam production requires additional resources and equipment. Associated oil/water/foam production control procedure is also too complex.
The claimed method allows to optimize preheating stage and reduce resource—, capital and energy costs. A saturated or a superheated steam is injected at an initial injection pressure into a tubing placed inside a well drilled in an oil reservoir. The steam temperature is measured at an outlet of the tubing and a heat flow from the well to the reservoir is calculated. Then, an optimal steam injection rate, when steam quality of the injected steam at the tubing outlet becomes greater than zero, is calculated, the optimal steam injection rate ensures compensation of the heat flow from the well to the oil-bearing formation with the heat of steam condensation. The steam injection rate is decreased to the calculated optimal steam injection rate value by decreasing the initial pressure providing constant temperature at the outlet of the tubing.
The saturated steam could be water based. The steam temperature at the outlet of the tubing can be measured constantly and continuously or periodically.
Additionally, a steam pressure can be measured at the outlet of the tubing.
The heat flow from well to the oil reservoir can be calculated by formulae:
where π is mathematical constant approximately equal to 3,14159, λ and a—thermal conductivity and thermal diffusivity of the oil reservoir, ΔT—difference between a temperature of a wall of the well determined from the measured steam temperature and the oil reservoir temperature, zhor—a length of a horizontal part of the well, t—a preheating time, rw—well radius, C1—constant value approximately equal to 1.
At the start of the preheating process it is preferable to set the initial injection pressure to the maximum possible value.
The claimed invention is illustrated by
According to the method a temperature is measured in a well drilled in an oil reservoir. Temperature data is used for estimation of a saturated steam temperature in the well. The heat flow from the well to the reservoir is calculated by an analytical formula using the measured steam temperature and reservoir thermal properties. A steam rate needed for an optimal operation regime is calculated on the basis of the energy balance. An optimal preheating time can be calculated by an analytical formula using reservoir thermal properties.
Presented workflow provides information on the steam rate needed for efficient and cost-effective SAGD preheating and optimal duration of the preheating with the respect to the reservoir thermal properties.
Main parameters of this model are: reservoir thermal conductivity and volumetric heat capacity, specific heat of steam condensation, steam quality, water density, difference between steam and reservoir temperature, well radius and length.
At the initial stage (1-7 days, depending on reservoir thermal properties) the rate of steam injection and hence an initial steam injection pressure are supposed to be as high as possible. A saturated or a superheated steam can be used.
At this stage due to the limitations of the well completion steam flow rate is lower than needed for optimal regime: achievable steam circulation rates often cannot compensate the heat flow from the well to the reservoir with the heat of the condensation as the reservoir is not heated. All this leads to the steam condensation in the tubing.
In order to control the preheating process Distributed Temperature Sensors (DTS) or ordinary sensors could be installed along the well. Temperature measurements can be carried out continuously or periodically. Time periods between measurements could depend on oil viscosity, reservoir properties, duration of the preheating and could vary from 1 to 10 times per day. At least one temperature sensor at an outlet of the tubing allows maintaining approximately constant steam temperature in the annulus in order to keep the same efficiency of the reservoir heating.
At the time moment when steam finally reaches the tubing outlet its saturation temperature will correspond to the particular saturation pressure at each point of the well. In one of the embodiments of the disclosed method steam state control could be done using additionally installed pressure sensors at the tubing outlet, example of applicable pressure sensor is listed in (Chalifoux G. V., Taylor R. M. Reservoir Monitoring Methods and Installation Practices//Canadian Association of Drilling Engineers newsletter, 2007, N.2. P. 2-5).
For the estimation of the heat flow from the well surface to the reservoir different numerical and analytical solutions could be used, in particular the analytical estimation of the heat flow from the cylindrical well surface to the reservoir. A temperature of a well wall can be determined using the measured temperature of saturated steam. The heat flow from well to the oil reservoir can be calculated by formulae:
where π is mathematical constant approximately equal to 3,14159, λ and a—thermal conductivity and thermal diffusivity of formation, ΔT—difference between the well wall temperature and a reservoir temperature, zhor—well horizontal section length, t—a preheating time, rw—well radius, C1—constant value approximately equal to 1.
In order to provide effective heating of the reservoir it is crucial to maintain sufficient amount of steam providing heat flow Q(t) (1). Heat is mainly delivered to the reservoir with the heat of steam condensation. Using the difference between steam quality values at the tubing inlet and annulus outlet (value at the outlet must be greater than zero and fixed at the relatively small value≈0.1) one can calculate steam rate W(t) needed for the optimal operation regime.
where L is a specific heat of steam condensation, ΔX=X0-X1, X0—steam quality at the tubing inlet, X1—steam quality at the annulus outlet (X1>0).
Thus as shown in (2) the optimal steam injection rate in time (after the steam quality at the annulus start to be greater than zero) should be determined by the condition that the heat flow from the well to the reservoir is compensated with the heat of steam condensation.
In the process of the reservoir preheating the heat flow rate from the well to the reservoir is decreasing in time as shown in
Optimal preheating duration can be determined using the analytical formula which depends on the reservoir thermal properties:
where h—half of a distance between wells, Cp—reservoir volumetric heat capacity, C2—dimensionless constant≈1, dependent on the chosen preheating temperature in the end of preheating process. C2 depends on the initial reservoir temperature and temperature between wells required to obtain oil mobility in interwell region. Time needed to preheat area between wells up to the temperature, for example, T=80 deg C. was calculated numerically and analytically using formula (3) (with C2=1.1) as presented in Table 1 (set of parameters described in the Example section).
The claimed method was implemented using commercial reservoir simulator with the following set of parameters (representing one of the Atabacka tar sands heavy oil fields):
Injection well parameters: length of horizontal section 500 m, the values of internal diameter (ID) and outer diameter (OD) of the annulus and tubing: ID tubing 3″, OD tubing 3.5″, ID casing 8.625″, OD casing 9.5″. The heat capacity of tubing/casing is 1.5 kJ/kg/K. Thermal conductivity of tubing/casing is 45 W/m/K, the wellbore wall effective roughness 0.001 m.
Optimal preheating duration was determined using the analytical formulae (3). For presented parameters preheating time was 60 days. During the whole simulation process temperature at the tubing outlet was constantly measured. Duration of the initial stage of the preheating process was 5 days. After that time steam temperature at the tubing outlet reached 180° C. Steam pressure value corresponded to this temperature was equal to 1.0 MPa. After the initial stage optimal steam injection rate W(t) was estimated using (2) and supported by the gradual decrease of the steam injection pressure. The claimed method allowed reducing total steam consumption by more than 50%.
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/RU2010/000456 | 8/23/2010 | WO | 00 | 4/22/2013 |
