Systems and methods for estimating and controlling liquid level using periodic shut-ins

Abstract

Methods and systems for determining a liquid level in a formation between a horizontal segment of an injection wellbore and a horizontal segment of a production wellbore are disclosed. Under shut-in conditions, local temperatures and pressures are determined for each of a plurality of inflow zones along the production wellbore segment. Local profile values are determined based on local shut-in subcool values and local shut-in liquid levels. After flow has resumed, a local liquid level is determined based on the local operating subcool value and the local profile value for that inflow zone. The local profile values may be updated during subsequent shut-ins.

Description

CROSS-REFERENCE TO RELATED APPLICATION

This application claims priority from Canadian Patent Application 2,983,541 filed Oct. 24, 2017 entitled SYSTEMS AND METHODS FOR DYNAMIC LIQUID LEVEL MONITORING AND CONTROL, and Canadian Patent Application 3,020,827 filed Oct. 15, 2018 entitled SYSTEMS AND METHODS FOR ESTIMATING AND CONTROLLING LIQUID LEVEL USING PERIODIC SHUT-INS, the entirety of which are incorporated by reference herein.

FIELD

This disclosure relates generally to monitoring liquid levels during petroleum extraction, and more specifically to systems and methods for utilizing distributed pressure and temperature measurements taken during shut-in conditions to determine local profile values, and to subsequently use the determined profile values and distributed temperature measurements taken along the production wellbore during operating conditions to determine the liquid level in the formation above the horizontal section.

BACKGROUND

Generally speaking, gravity drainage refers to a recovery process in which gravity is the primary force used to recover heavy oil and bitumen from a reservoir. An example of a gravity drainage process is Steam Assisted Gravity Drainage (SAGD). In a typical SAGD process, two horizontal wellbores are drilled into an oil-containing reservoir. The wellbores are positioned generally parallel to each other and spaced apart vertically, with one wellbore being positioned above the other wellbore, typically by about 4 to 6 meters. During production, high pressure steam is injected into the upper wellbore (also referred to as the injector) to heat the oil in the surrounding formation, thereby reducing its viscosity such that it can flow through the formation under the force of gravity. The heated oil—along with any condensed steam (i.e. water)—drains into the lower wellbore (also referred to as the producer), and the collected oil and water are pumped to the surface.

Solvent Assisted—Steam Assisted Gravity Drainage (SA-SAGD) and Vapor Assisted Petroleum Extraction (VAPEX) are examples of other gravity drainage recovery processes for producing heavy oil. SA-SAGD and VAPEX are similar to SAGD, but instead of (or in addition to) steam, one or more vaporized solvents (e.g. ethane, propane) are injected to reduce the viscosity of oil in the surrounding formation.

SUMMARY

The following introduction is provided to introduce the reader to the more detailed discussion to follow. The introduction is not intended to limit or define any claimed or as yet unclaimed invention. One or more inventions may reside in any combination or sub-combination of the elements or process steps disclosed in any part of this document including its claims and figures.

In accordance with one broad aspect of this disclosure, there is provided a method for determining a liquid level in a formation between a horizontal segment of an injection wellbore and a horizontal segment of a production wellbore, the method comprising: shutting-in the production wellbore; shutting-in the injection wellbore; measuring, using at least one first temperature sensor positioned in the production wellbore segment, a local shut-in temperature for each of a plurality of inflow zones between a heel and a toe of the production wellbore segment; measuring, using at least one first pressure sensor positioned in the production wellbore segment, a local shut-in pressure for each of the plurality of inflow zones; determining, for each of the plurality of inflow zones: a local shut-in liquid level, based on the measured shut-in pressure at that inflow zone and a shut-in pressure for an injection zone horizontally aligned with that inflow zone; a local shut-in subcool value, based on the measured shut-in temperature at that inflow zone; and a local profile value, based on the local shut-in subcool value for that inflow zone and the local shut-in liquid level for that inflow zone; resuming flow in the production wellbore; resuming flow in the injection wellbore; after resuming flow in the production and injection wellbores, for at least one of the plurality of inflow zones: measuring, using the at least one first temperature sensor positioned in the production wellbore, a local operating temperature for that inflow zone; determining a local operating subcool value, based on the measured operating temperature at that inflow zone; determining a local operating liquid level, based on the local operating subcool value for that inflow zone and the local profile value for that inflow zone.

In some embodiments, a local operating liquid level is determined for each of the plurality of inflow zones.

In some embodiments, the determined local shut-in subcool value is based on a local saturation temperature of an injection fluid at the measured shut-in pressure at that inflow zone and the measured shut-in temperature at that inflow zone.

In some embodiments, the method further comprises, after resuming flow in the production and injection wellbores, measuring, using the at least one first pressure sensor, a local operating pressure for that inflow zone, and the determined local operating subcool value is based on a local saturation temperature of the injection fluid at the measured operating pressure at that inflow zone and the measured operating temperature at that inflow zone.

In some embodiments, the determined local operating liquid level is based on the local shut-in liquid level for that inflow zone, a difference between the local operating subcool value for that inflow zone and the local shut-in subcool value for that inflow zone, and the local profile value for that inflow zone.

In some embodiments, the local shut-in temperature for each of the plurality of injection zones is obtained using at least one second temperature sensor positioned in the injection wellbore.

In some embodiments, the local shut-in pressure for each of the plurality of injection zones is obtained using at least one second pressure sensor positioned in the injection wellbore.

In some embodiments, the method further comprises: after determining the local operating liquid level for the at least one of the plurality of inflow zones: comparing the determined local operating liquid level for the at least one of the plurality of inflow zones to a target liquid level; in response to the determined local operating liquid level for the at least one of the plurality of inflow zones being greater than the target liquid level, performing at least one of: increasing a pump rate of an artificial lift device to increase the total flowrate for fluids exiting the production wellbore segment; increasing an open area of at least one of the plurality of inflow zones; and unblocking the open area of at least one of the plurality of inflow zones; and in response to the target liquid level being greater than the determined local operating liquid level for the at least one of the plurality of production zones, performing at least one of: decreasing the pump rate of the artificial lift device to decrease the total flowrate for fluids exiting the production wellbore segment; decreasing the open area of at least one of the plurality of inflow zones; and blocking the open area of at least one of the plurality of inflow zones.

In some embodiments, in response to the determined local operating liquid level for at least one of the plurality of inflow zones being greater than the target liquid level, the method further comprises increasing an injection rate of a fluid injector to increase a total flow rate of fluids into the injector wellbore, in order to maintain pressure in a steam chamber.

In some embodiments, in response to the determined local operating liquid level for at least one of the plurality of inflow zones being greater than the target liquid level, the method further comprises decreasing an injection rate of a fluid injector to decrease a total flow rate of fluids into the injector wellbore, in order to decrease a bitumen drainage rate in a steam chamber.

In some embodiments, in response to the target liquid level being greater than the determined local operating liquid level for at least one of the plurality of inflow zones, the method further comprises decreasing an injection rate of a fluid injector to decrease a total flow rate of fluids into the injector wellbore, in order to maintain pressure in a steam chamber.

In some embodiments, in response to the target liquid level being greater than the determined local operating liquid level for at least one of the plurality of inflow zones, the method further comprises increasing an injection rate of a fluid injector to increase a total flow rate of fluids into the injector wellbore, in order to increase a bitumen drainage rate in a steam chamber.

In some embodiments, the method further comprises: after determining the local operating liquid level for the at least one of the plurality of inflow zones: shutting-in the production and injection wellbores a second time; determining updated local profile values for each of the plurality of inflow zones; resuming flow in the production and injection wellbores a second time; after resuming flow in the production and injection wellbores the second time, for at least one of the plurality of inflow zones: determining an updated local operating liquid level, based on an updated local shut-in liquid level for that inflow zone, a difference between an updated local operating subcool value for that inflow zone and an updated local shut-in subcool value for that inflow zone, and the updated local profile value for that inflow zone.

In some embodiments, the method further comprises: after determining the local profile values during a first shut-in period: determining updated local profile values during a second shut-in period; determining, for at least one of the plurality of inflow zones, a profile adjustment factor based on the local profile value for that inflow zone, the updated local profile value for that inflow zone, and a duration between the first and second shut-in periods; and after resuming flow in the production and injection wellbores following the second shut-in period, for at least one of the plurality of inflow zones: determining a local operating liquid level, based on the local shut-in liquid level for that inflow zone, a difference between the local operating subcool value for that inflow zone and the local shut-in subcool value for that inflow zone, the updated local profile value for that inflow zone, the profile adjustment factor for that inflow zone, and a duration between the second shut-in period and a period during which the local operating temperature and pressure were measured when determining the subcool value for that inflow zone.

In some embodiments, the method further comprises: after shutting in the injection wellbore, and before determining the local shut-in liquid levels: performing a gas purge of the injector wellbore.

In accordance with another broad aspect, there is provided a system for determining a liquid level in a formation between a horizontal segment of an injection wellbore and a horizontal segment of a production wellbore, the system comprising: at least one first temperature sensor positioned in the production wellbore segment to measure a local temperature for each of a plurality of inflow zones between a heel and a toe of the production wellbore segment; at least one first pressure sensor positioned in the production wellbore segment to measure a local pressure for each of the plurality of inflow zones; one or more processors operatively coupled to the at least one first temperature sensor and the at least one first pressure sensor, the one or more processors, collectively, configured to: during a period in which the production wellbore and the injection wellbore are shut-in: determine, for each of the plurality of inflow zones: a local shut-in liquid level, based on a measured shut-in pressure at that inflow zone and a shut-in pressure for an injection zone horizontally aligned with that inflow zone; a local shut-in subcool value, based on a measured shut-in temperature at that inflow zone; and a local profile value, based on the local shut-in subcool value for that inflow zone and the local shut-in liquid level for that inflow zone; and after resuming flow in the production and injection wellbores: determine, for at least one of the plurality of inflow zones: a local operating subcool value, based on a measured operating temperature at that inflow zone; and a local operating liquid level, based on the local operating subcool value for that inflow zone and the local profile value for that inflow zone.

In some embodiments, the one or more processors are configured to determine the local shut-in subcool value for each of the plurality of inflow zones based on the measured shut-in temperature at that inflow zone and a local saturation temperature of an injection fluid at the measured shut-in pressure at that inflow zone.

In some embodiments, the one or more processors are configured to determine the local operating subcool value for the at least one of the plurality of inflow zones based on the measured operating temperature at that inflow zone and a local saturation temperature of the injection fluid at a measured operating pressure at that inflow zone.

In some embodiments, the one or more processors are configured to determine the local operating liquid level based on the local shut-in liquid level for that inflow zone, a difference between the local operating subcool value for that inflow zone and the local shut-in subcool value for that inflow zone, and the local profile value for that inflow zone.

In some embodiments, the at least one first temperature sensor comprises a thermocouple or a set of thermocouples.

In some embodiments, the at least one first temperature sensor comprises a distributed temperature sensor (DTS).

In some embodiments, the system further comprises at least one second temperature sensor positioned in the injection wellbore to measure a local temperature for each of a plurality of injection zones between a heel and a toe of the injection wellbore segment.

In some embodiments, the at least one first pressure sensor comprises a distributed pressure sensing system.

In some embodiments, the at least one first pressure sensor is positioned exterior of a production string located in the production wellbore segment.

In some embodiments, the at least one first pressure sensor comprises fewer discrete pressure sensors than the number of inflow zones in the plurality of inflow zones, and wherein, for inflow zones without a discrete pressure sensor positioned therein, the one or more processors are configured to determine local pressures for those inflow zones using a model based on pressures from discrete pressure sensors positioned in other inflow zones.

In some embodiments, the system further comprises at least one second pressure sensor positioned in the injection wellbore to measure a local pressure for each of the plurality of injection zones.

In some embodiments, the at least one second pressure sensor comprises fewer discrete pressure sensors than the number of injection zones in the plurality of injection zones, and wherein, for injection zones without a discrete pressure sensor positioned therein, the one or more processors are configured to determine local pressures for those injection zones using a model based on pressures from discrete pressure sensors positioned in other injection zones.

In some embodiments, the plurality of inflow zones comprises at least five inflow zones.

In some embodiments, the system further comprises a display device operatively coupled to the one or more processors, and the one or more processors are further configured to cause the display device to display a graphical representation of the determined local operating liquid levels for the at least one of the plurality of inflow zones.

In some embodiments, the graphical representation of the determined local operating liquid levels for the at least one of the plurality of inflow zones comprises a representation of local operating liquid levels for at least ten percent of a length between the heel and the toe of the production wellbore segment.

It will be appreciated by a person skilled in the art that a method or apparatus disclosed herein may embody any one or more of the features contained herein and that the features may be used in any particular combination or sub-combination.

These and other aspects and features of various embodiments will be described in greater detail below.

BRIEF DESCRIPTION OF THE DRAWINGS

For a better understanding of the described embodiments and to show more clearly how they may be carried into effect, reference will now be made, by way of example, to the accompanying drawings in which:

FIG. 1 is a schematic axial cross-section view of a pair of horizontal wellbores through a formation being used in a typical gravity drainage recovery process;

FIG. 2 is a schematic longitudinal cross-section view of the horizontal wellbores of FIG. 1, with a first liquid level and a first estimated liquid level;

FIG. 3 is the schematic longitudinal cross-section view of FIG. 2, with a second liquid level and a second estimated liquid level;

FIG. 4 is a schematic longitudinal cross-section view of a pair of horizontal wellbores in accordance with one example embodiment;

FIG. 5 is a schematic longitudinal cross-section view of a pair of horizontal wellbores in accordance with another example embodiment;

FIG. 6 is a schematic longitudinal cross-section view of a pair of horizontal wellbores in accordance with another example embodiment;

FIG. 7 is a schematic longitudinal cross-section view of a pair of horizontal wellbores in accordance with another example embodiment;

FIG. 8 is a simplified process flow diagram for a method for determining a liquid level in a formation between a horizontal segment of an injection wellbore and a horizontal segment of a production wellbore in accordance with one embodiment;

FIG. 9 is a schematic illustration of an estimated liquid level between a pair of horizontal wellbores;

FIG. 10 is a plot of simulation results for local liquid level height as a function of pressure during a simulated SAGD operation;

FIG. 11 is a plot of simulation results for local liquid level height as a function of local subcool during a simulated SAGD operation; and

FIG. 12 is a plot of simulation results for a local profile value as a function of time during a simulated SAGD operation.

The drawings included herewith are for illustrating various examples of articles, methods, and apparatuses of the teaching of the present specification and are not intended to limit the scope of what is taught in any way.

DETAILED DESCRIPTION

Various apparatuses, methods and compositions are described below to provide an example of an embodiment of each claimed invention. No embodiment described below limits any claimed invention and any claimed invention may cover apparatuses and methods that differ from those described below. The claimed inventions are not limited to apparatuses, methods and compositions having all of the features of any one apparatus, method or composition described below or to features common to multiple or all of the apparatuses, methods or compositions described below. It is possible that an apparatus, method or composition described below is not an embodiment of any claimed invention. Any invention disclosed in an apparatus, method or composition described below that is not claimed in this document may be the subject matter of another protective instrument, for example, a continuing patent application, and the applicant(s), inventor(s) and/or owner(s) do not intend to abandon, disclaim, or dedicate to the public any such invention by its disclosure in this document.

Furthermore, it will be appreciated that for simplicity and clarity of illustration, where considered appropriate, reference numerals may be repeated among the figures to indicate corresponding or analogous elements. In addition, numerous specific details are set forth in order to provide a thorough understanding of the example embodiments described herein. However, it will be understood by those of ordinary skill in the art that the example embodiments described herein may be practiced without these specific details. In other instances, well-known methods, procedures, and components have not been described in detail so as not to obscure the example embodiments described herein. Also, the description is not to be considered as limiting the scope of the example embodiments described herein.

FIG. 1 illustrates a schematic axial cross-section of a typical SAGD recovery process. A pair of parallel horizontal wellbore segments 100, 200 are provided in a formation or reservoir 10 and are spaced apart vertically by a distance d. Steam is pumped down from the surface and along the upper wellbore 100, where it passes into the formation 10 via one of a number of apertures 110 (e.g. screens, perforations) provided in the wellbore casing. Upper wellbore 100 may also be referred to as an injector wellbore or simply an injector. As steam is injected, thermal energy from the steam is transferred to the formation. This thermal energy increases the temperature of petroleum products present in the formation (e.g. heavy crude oil or bitumen), which reduces their viscosity and allows them to flow downwards under the influence of gravity towards the lower wellbore 200, where it passes into the wellbore 200 via one of a number of apertures 210 (e.g. screens, perforations) provided in the wellbore casing. Lower wellbore 200 may also be referred to as a producer wellbore or simply a producer.

As the steam initially enters the reservoir, a ‘steam chamber’ 20 is formed. The boundary or wall 22 of the steam chamber represents a boundary between fluids in a gaseous state (including injected steam—as indicated by arrows 12—and any gasses present in the formation) and fluids in a liquid state (including heavy crude oil or bitumen and condensed steam). As steam injection continues, thermal energy is released from the steam as it condenses against the wall 22 of the steam chamber. Heated petroleum products and condensate (as indicated by arrows 14) flow along or adjacent to the wall 22, and down into producer wellbore 200. Within the steam chamber, fluids in a gaseous state tend to rise towards the top of the chamber 24 due to their relatively low density, while liquids tend to collect at the bottom of the steam chamber 26. In the illustrated example, the liquid level at the bottom of the steam chamber is a distance h above the producer wellbore 200.

While during normal operation lower wellbore 200 acts as a producer (i.e. fluid is extracted from the formation via wellbore 200), it will be appreciated that wellbore 200 may alternately act as an injector. For example, during start-up of an SAGD process steam may be pumped into both wellbores 100 and 200 to initially heat the formation proximate both the upper and lower wellbores, following which wellbore 200 may be transitioned to a producer by discontinuing the steam flow into this wellbore.

FIG. 2 illustrates a schematic longitudinal cross-section of a typical SAGD recovery process. Steam is pumped down from the surface through the vertical section 102 and the heel 104 of the injector wellbore 100, and along the horizontal segment 106 towards the toe 108. A number of outflow locations 110 (e.g. screens, perforations, or other apertures) are provided along the injector wellbore casing to allow the steam to access the formation. Heated petroleum products and condensate from the injected fluids flow down through the formation 10 and into producer wellbore 200 through one of a number of inflow locations 210 (e.g. screens, perforations, or other apertures) provided along the horizontal segment 206 of the producer wellbore casing between the heel 204 of the producer wellbore and the toe 208. One or more artificial lift devices 300 (e.g. electrical submersible pumps) is used to pump fluids collected along the horizontal segment 206 of the producer wellbore 200 up to the surface through the vertical section 202.

In the illustrated example, the line 50 represents the liquid level h in the formation (e.g. the level of the liquid at the bottom of the steam chamber) above the producer wellbore 200 along its horizontal segment. As shown, the liquid level h typically varies along the length of the horizontal wellbore segment due to local differences in one or more parameters, such as porosity of the formation, temperature and pressure levels, composition of petroleum products, etc.

In the example illustrated in FIG. 2, the liquid level h is above the producer wellbore at all points along the horizontal segment 206. Accordingly, the fluids entering the producer wellbore through apertures 210 are in their liquid phase. This is typically considered to be a preferable operating condition, as artificial lift devices (e.g. a rod pump or an electric submersible pump) are generally much more efficient when pumping liquids than when pumping a mix of liquid and gas. For example, pumping fluids in a gas phase may be less efficient than pumping liquids, resulting in increased energy expenditures to extract the fluids to the surface. Also, pumping gasses may lead to increased wear and/or maintenance requirements for the lift device, and may result in a reduced operating lifespan.

In a typical SAGD process, the liquid level h is approximated by comparing the temperature of the injected steam (e.g. the saturation temperature or boiling point of water at the operating pressure of the injector) to the temperature of the fluids exiting the horizontal segment of the producer wellbore 206. For example, a temperature sensor 320 may be provided proximate the heel 204 of the wellbore 200 and/or proximate the artificial lift device 300 to obtain a temperature value for the fluids being produced. The difference between these temperatures is often referred to as the ‘subcool’. (It will be appreciated that the term ‘subcool’ may have one or more alternative definitions, and may be used in other contexts to refer to similar, or unrelated, concepts. For example, some operators may determine a distributed temperature and define a ‘reservoir subcool’ as the local difference between the reservoir temperature and the distributed temperature.) A higher subcool (i.e. a greater difference in injection and production temperatures) is considered indicative of a higher liquid level in the formation, while a lower subcool is considered indicative of a lower liquid level. Put another way, the subcool is used as a proxy for the liquid level. In FIG. 2, line 60 illustrates an example approximation of a liquid level h′ based on the subcool.

If the subcool is low, indicating a lower liquid level, the pump rate of the artificial lift device 300 may be reduced to decrease the flow rate out of the horizontal segment. Reducing the pump rate may also result in increased pressure along the horizontal segment 206 of the producer wellbore 200 as a result of increasing liquid level in the reservoir and reduced frictional pressure drop within the well. A reduction in flowrate and/or increase in pressure for the producer can be expected to result in an increased liquid level in the formation, and accordingly a reduced risk of steam coning.

Conversely, if the subcool is high, this may result in an increased potential to ‘flood’ the injector wellbore. Also, a higher subcool (and the attendant higher liquid level) may indicate a less than optimum production rate. Also, a high subcool may result in reduced production, as fluids (e.g. heavy oil or bitumen) entering the producer at lower temperatures would be expected to have a higher viscosity and lower mobility. Accordingly, if the subcool is high the pump rate of the artificial lift device 300 may be increased to increase the flow rate out of the horizontal segment, and/or to reduce the pressure along the horizontal segment 206 of the producer wellbore 200. An increase in flowrate and/or decrease in pressure for the producer can be expected to increase production from the formation, which may be desirable given a reduced risk of steam coning due to the relatively high liquid level.

While the subcool can be used to approximate the liquid level, this estimation may have one or more limitations. For example, the single temperature value for the fluids being produced is an average temperature for fluids along the entire wellbore segment, and therefore may fail to capture local temperature variations. Thus, the liquid level is assumed to be approximately constant along the entire length of the horizontal segment. This can make it difficult to detect steam coning or other undesirable conditions.

For example, FIG. 3 illustrates another schematic longitudinal cross-section of a SAGD recovery process. In this example, the liquid level h is above the producer wellbore at inflow locations 210_a-210_d and 210_h-210_q along the horizontal segment 206, but it is below the producer wellbore at inflow locations 210_e-210_g. Accordingly, while fluids entering the producer wellbore at inflow locations 210_a-210_d and 210_h-210_q are in their liquid phase, at least some of the fluids entering the producer wellbore at inflow locations 210_e-210_g are in a gaseous phase. In other words, some of the steam injected from the injector wellbore effectively ‘short circuits’ through the formation and passes into the producer. This situation may be characterized as ‘steam coning’, and is typically considered to be a less preferable operating condition. For example, as a result of this steam ‘bypass’, less thermal energy may be transferred to the formation.

In the example illustrated in FIG. 3, fluid entering the producer at inflow locations 210_e-210_g will comingle with fluid entering the producer at inflow locations 210_a-210_d and 210_h-210_q before a temperature is sensed by the temperature sensor 320. This comingling may mute any local temperature variance, as the temperature sensor 320 only detects an average temperature of the producer fluid. Accordingly, local inflow temperatures indicative of steam coning may not be detected based on the subcool. Instead, steam coning may be detected based on an increase in the percentage of water (or other injected fluids) in the produced fluids, e.g. when sampled at the surface. Alternatively, steam coning may be detected when the inflow to the artificial lift device 300 contains fluids in both liquid and gaseous phases, e.g. as indicated by the pump registering a fault condition. Alternatively, thermocouples or DTS fiber may provide direct detection methods for steam coning, as a local temperature value above a predetermined threshold may be indicative of steam coning at that location (although knowing a location of steam coning typically does not provide sufficient information to predict a liquid level away from the coning point). Each of these detection methods may be characterized as reactive detection, in that steam coning is only detected after it has occurred.

FIG. 4 illustrates a schematic longitudinal cross-section of a pair of horizontal wellbores that are provided with sensors for measuring temperature and pressure at a number of inflow locations 210_a-210_g distributed along the length of the horizontal segment 206 of the producer 200. While 17 inflow locations are shown, it will be appreciated that more or fewer inflow locations may be provided in a horizontal segment 206. In this example, each inflow location 210 is also considered to be an inflow zone 215. As discussed further below, by obtaining pressure and temperature data for a number of zones along the horizontal segment 206 of the producer wellbore, this may allow a more accurate and/or more detailed model of the reservoir conditions surrounding the wellbores, including the liquid level h above the producer, to be developed. A more accurate model of the liquid level h may allow for improved control of production during a SAGD process.

In the example illustrated in FIG. 4, each inflow location 210 (and zone 215) to the producer has an associated temperature sensor 220. Each temperature sensor 220_a-220_g may be a discrete unit, such as a thermocouple, resistive thermal device (RTD), and the like. Alternatively, a distributed temperature sensor (DTS) may be used to obtain temperature data for each inflow location 210_a-210_q. For example, a sensor based on Optical Time Domain Reflectometry (OTDR) or Optical Frequency Domain Reflectometry (OFDR) may be used. For each inflow location, the local temperature in the reservoir adjacent the inflow location T_{res_inflow} may be assumed as being equal to a temperature value T_inflow measured by a temperature sensor 220, or may be based on a measured temperature value T_inflow subject to an adjustment factor (e.g. to compensate for a temperature drop across the reservoir/wellbore interface).

Also, in the example illustrated in FIG. 4 each inflow location 210 (and zone 215) has an associated pressure sensor 230_a-230_q. Each pressure sensor may be a discrete unit, such as a quartz-based sensor, bubble tube, electromagnetic resonating element (ERE), electrical resonating diaphragm, and the like. Alternatively, a distributed pressure sensing system incorporating one or more distributed Fiber Bragg Grating pressure sensors may be used to obtain pressure data for each inflow location 210_a-210_q. Alternatively, multiple individual Fabry Perot gauges connected to the same fiber optic trunkline may be used to obtain pressure data for each inflow location 210_a-210_q or inflow zone 215_a-215_q. For example, a sensor system such as a SageWatch™ Subsurface Surveillance System, available from SageRider, Inc., or the like may be used. For each inflow location, the local pressure in the reservoir adjacent the inflow location P_{res_inflow} may be assumed as being equal to a pressure value P_inflow measured by a pressure sensor 230, or may be based on a measured pressure value P_inflow subject to an adjustment factor (e.g. to compensate for a pressure drop across the reservoir/wellbore interface).

Preferably, one or more of the pressure sensors 230 are connected directly to the formation. For example, they may be positioned exterior of a production string located in the production wellbore segment. Positioning one or more of the pressure sensors 230 in direct connection with the reservoir may improve the accuracy of the local reservoir pressure measurements. For example, local pressure measurements taken using sensors positioned in a pipe (e.g. inside a production string) may be impacted by pressure equilibration upstream and downstream due to fluid flow in the pipe. Also, in areas where there is active pressure communication (e.g. near an inflow location or an inflow control device) pressure measurements taken using sensors positioned inside a production string may be impacted by the upstream and downstream pressures in the pipe. For example, there may be a drop in measured pressure during a period of transient flow following a shut-in while the pressure equilibrates.

Optionally, pressure sensors 230 connected directly to the formation (e.g. positioned exterior of a production string located in the production wellbore segment) may be positioned approximately midway between adjacent inflow locations and/or inflow control devices along the production wellbore segment. In such locations, the influence of pressure communication within the well fluids may be reduced or preferably minimized, and thus improve and preferably maximize the correlation between the pressure measurements recorded using the pressure sensors 230 and the actual reservoir pressure.

In some examples, a distributed data acquisition system may include one or more multi-function sensors capable of obtaining both pressure and temperature data at each inflow location 210_a-210_q and/or for each inflow zone 215_a-215_q. Accordingly, the same physical sensor apparatus may function as both a pressure sensor and as a temperature sensor to obtain pressure and temperature data for one or more locations along the wellbore. For example, sensor systems such as CT-MORE, available from Core Laboratories of Houston, Tex., or CanePT™ Optical Pressure and Temperature Sensor, available from Weatherford International, or the like may be used.

In the example illustrated in FIG. 4, each inflow zone 215 is shown with a single aperture 210 to the producer. Alternatively, some or all of the inflow zones may include more than one discrete aperture through which fluids can enter the producer from the formation. FIG. 5 illustrates a schematic longitudinal cross-section of a pair of horizontal wellbores that are provided with sensors for measuring temperature and pressure at a number of inflow zones 215_a-215_f distributed along the length of the horizontal segment 206 of the producer 200. In the illustrated example, each inflow zone 215_a-215_e includes three apertures 210 through which fluid can enter the producer from the formation, and inflow zone 210_f includes two such apertures. It will be appreciated that each zone may have more or fewer apertures.

In the example illustrated in FIG. 4, each inflow zone 215 to the producer is shown with an associated temperature and pressure sensor. Alternatively, one or more of the inflow zones may not include a discrete pressure sensor. For example, discrete temperature sensors (or a distributed temperature sensor) may be provided to measure local temperatures at every 1 meter or so along the production wellbore, while discrete pressure sensors (or a distributed pressure sensing system) may be provided to measure local pressure values at every 10 meters or so along the production wellbore.

FIG. 6 illustrates a schematic longitudinal cross-section of a pair of horizontal wellbores that are provided with sensors for measuring temperature and pressure for a number of inflow zones 215_a-215_g distributed along the length of the horizontal segment 206 of the producer 200. In the illustrated example, pressure sensors 230_a-230_g are provided at, respectively, inflow locations 210_b, 210_e, 210_i, 210_m, 210_o, 210_p, and 210_q, such that each inflow zone 215_a-215_g is centered around a respective pressure sensor 230_a-230_g.

In some embodiments, the locations of pressure sensors 230_a-230_g may be determined based on the geology of the formation. For example, a single pressure sensor 230 may be positioned at the approximate midpoint of a region of relatively constant porosity, as the formation pressure along such a region may be expected to be relatively constant.

In the example illustrated in FIG. 6, each inflow zone 215 is centered around a respective pressure sensor 230. Alternatively, to determine a local pressure value for inflow zones that do not have a pressure sensor positioned therein, a flow model (e.g. using pressure data from sensors at one or more other inflow zones) may be used. For example, a local pressure value for an inflow zone 215 may be determined using a flow model that computes pressure values along the production wellbore between the locations of pressure sensors 230 positioned in adjacent inflow zones.

In the example illustrated in FIG. 4, each inflow location 210 or zone 215 along the producer has an associated temperature sensor 220 and an associated pressure sensor 230. In the example illustrated in FIG. 7, each injection location or zone 115 along the injector also has an associated temperature sensor 120 and an associated pressure sensor 130. As with the sensors for the producer, each pressure sensor and/or each temperature sensor may be a discrete unit, or a distributed data acquisition system may be used to obtain temperature and/or pressure data at each injection zone 115. That is, the same physical sensor apparatus may function as both a pressure sensor and as a temperature sensor at one or more locations along the injector wellbore.

By obtaining pressure and temperature data for a number of locations or zones distributed along the horizontal segment of the producer wellbore during shut-in conditions, local liquid levels may be estimated along the horizontal length of the well pair (which may account for local heterogeneities in the formation). This may allow a more accurate and/or more detailed baseline model to be developed for the reservoir conditions (e.g. liquid level) along the wellbore. A more accurate baseline model may allow for improved control of production during a gravity drainage process (e.g. SAGD).

For example, during normal operation, pressure at any given location along the producer wellbore is a function of: i) the fluid head between the injector and producer; ii) the pressure drop across the completion (including any skin effects); iii) the thermodynamic state of the fluid; iv) the frictional pressure loss along the wellbore segment between locations, which may be determined as a direct function of the vapor and liquid fractions of the fluids (which can be determined e.g. from a thermodynamic equilibrium calculation or a non-equilibrium calculation) and the flow rate through the producer wellbore; and v) while flowing, the pressure also depends on the Darcy's Law pressure drop due to the viscous effects of fluid flowing through porous media.

However, when the well is shut-in, the flow effects quickly become negligible (e.g. drop to zero) leaving the fluid head between the injector and producer as the only component of pressure. It should be recognized that the fluid head is the sum of the reservoir pressure and the height of liquid above the producer. Accordingly, a reasonable estimation of the liquid level for a given location or zone above the producer wellbore may be made using temperatures and ‘static’ pressures measured under shut-in conditions, and an assumed fluid composition (e.g. as obtained from a calibration of the producing well model, or obtained from sampling produced fluids during operation). Such ‘local’ estimates of liquid levels may be combined to form a more detailed and/or more accurate estimate of the liquid level as it varies along the length of the producer wellbore at the time the wells are shut-in.

Also, by obtaining pressure and temperature data for a number of locations or zones distributed along the horizontal segment of the producer wellbore during shut-in conditions, local profile values may be estimated for the well pair (which may account for local heterogeneities in the formation). These profile values may be characterized as a relationship between a subcool change and a change in the liquid level (e.g. a change in local subcool corresponding to a 1 m change in a local liquid level). Once production has resumed following the shut-in, local operating liquid levels may be estimated using local profile values in conjunction with local pressure and temperature measurements taken during operating conditions.

Accordingly, determining local operating temperatures and pressures for a number of locations or zones along the horizontal segment of a producer wellbore may allow for the determination of local subcool values, which, along with local profile values, may allow an improved calculation of local liquid levels between the injector wellbore and the producer wellbore. This may enable well pair operation based on local liquid levels estimated from local subcools, rather than a single average liquid level based on the average subcool.

A more accurate and/or more detailed model for the reservoir conditions (e.g. local liquid levels) along the wellbore may also facilitate faster identification and/or responses to system changes, which may have one or more advantages. For example, improved responses to system changes may allow for a more efficient use of steam or other injected fluids. Improved responses to system changes may also allow for improved run life for an ESP or other artificial lift device. Improved responses to system changes may also allow for lower temperature operations near inflow locations, which may improve the expected operating life of producer screens, as these screens may be ‘burnt through’ or otherwise damaged by prolonged exposure to direct steam production (e.g. if exposed to injector fluids that pass through the formation during ‘steam coning’).

Referring to FIG. 8, there is illustrated a method 800 for determining a liquid level in a formation between a horizontal segment of an injection wellbore and a horizontal segment of a production wellbore. Method 800 may be performed using apparatus as illustrated in FIGS. 4 to 7 or any other suitable apparatus.

At 805, the production wellbore and the injection wellbore are shut-in. Optionally, the injector may undergo a gas purge in order to reduce the liquid level in the injector annulus to obtain a more accurate bottom hole pressure for the injector wellbore from a wellhead pressure gauge. For example, an inert gas such as N₂ may be pumped into the injector wellbore to displace any condensed vapour present in the injector wellbore into the reservoir.

At 810, values for local shut-in temperatures (i.e. a temperature measured after the wellbore has been shut-in) for a plurality of inflow zones (e.g. T_{inflow_1} to T_{inflow_n} or T_{res_inflow} to T_{res_inflow} n for n zones), are measured using one or more temperature sensors distributed along the producer wellbore 200.

At 815, values for local shut-in pressures (i.e. a pressure measured after the wellbore has been shut-in) for a plurality of inflow zones (e.g. P_{inflow_1} to P_{inflow_n} or P_{res_inflow_1} to P_{res_inflow_n} for n zones), are measured using one or more pressure sensors distributed along the producer wellbore 200.

Optionally, at 820, values for local shut-in temperatures for a plurality of injection zones (e.g. T_{inj_1} to T_{inj_n} for n zones) may be measured using one or more temperature sensors distributed along the injector wellbore 100. Alternatively, a shut-in temperature for the injection zones may be estimated based on, e.g. wellhead measurements and/or a saturation curve for the injected fluid(s).

Optionally, at 825, values for local shut-in pressures for a plurality of injection zones (e.g. P_{inj_1} to P_{inj_n} for n zones), are measured using one or more pressure sensors distributed along the injector wellbore 100. Alternatively, a shut-in pressure for the injection zones may be estimated based on, e.g. wellhead measurements and/or a saturation curve for the injected fluid(s), or any other suitable method.

For example, under saturated conditions, the saturation curve for the injection fluid can be used to determine the saturation pressure as a function of saturation temperature and injected solvent concentration:P_sat=f(T_sat,Conc_solvent)  (1)Accordingly, under saturation conditions, a measurement of temperature provides a direct value for the saturation pressure. For example, for SA-SAGD, a temperature measurement and injected solvent concentration can be used to determine a pressure value.

As another example, for SAGD, assuming no pressure drop due to flow, and assuming that the injector wellbore is filled with steam, the static bottom hole pressure may be calculated using a pressure measurement taken at the wellhead and known steam properties:P_{bottom_hole}=P_wellhead+(ρ_steam)(g)(h)  (2)where ρ_steam is the density for steam and h is the height difference between the bottom hole location and the location of the wellhead measurement. Alternatively, if accumulated liquid is blown out with a gas (e.g. during a purge operation using N₂ gas), ρ_steam may be replaced with ρ_gas. Simulation results indicate that reservoir temperature/pressure at the injector is relatively uniform in areas of good steam conformance (i.e. where steam actually enters the formation). It will be appreciated that additional measurements (e.g. temperatures measured for an observation well associated with the injector/producer wellpair) may optionally be used to correct the estimation of the injector pressure.

It will be appreciated that the production and injection wellbores may be shut-in for a number of reasons, such as for periodic scheduled maintenance, or an unscheduled power outage. Preferably, steps 810 to 825 may be performed during an otherwise scheduled shut-in, as this may limit non-production time for the recovery process.

At 830, a local shut-in liquid level is determined under static flow conditions for each of the plurality of inflow zones. Preferably, the shut-in liquid level for an inflow zone is based on the measured shut-in pressure at that inflow zone, and a shut-in pressure for an injection zone horizontally aligned with that inflow zone.

For example, with reference to FIG. 9, the local liquid level h_i above an inflow location or zone may be determined based on the local reservoir pressure P_{res_i} as measured at 815, the local pressure in the injector wellbore P_{inj_i} at a point above the local reservoir location (e.g. as measured at 825 or as otherwise determined/estimated), and the local density of the fluid (which may be an assumed value—for example, the density of the fluid in the reservoir above the producer wellbore 200 may be estimated using P_{res_inflow_i} (or P_{inflow_i}), T_{res_inflow_i} (or T_{inflow_i}), and a known or expected composition of the fluid). For example, the local liquid level h_i may be determined using:

$\begin{array}{cc}{h}_i=\frac{P_{\mathrm{res}\_\mathrm{inflow}\_i}-P_{\mathrm{inj}\_i}}{{\rho }_L\times g}& \left(3\right)\end{array}$ where g is the gravitational constant, and ρ_L is the density of the liquid in the reservoir. For example, density may be measured at the surface, either with online instruments or with collected samples, and these surface values may then be corrected to bottom hole conditions (e.g. by assuming that the surface composition is the same as the composition in the reservoir).

For some processes (e.g. the injection of pure steam, or a pure solvent such as pentane, hexane, etc.), the local pressure in the injector wellbore P_{inj_i} may be assumed constant over the entire length of the wellbore (e.g. P_{inj_i}=P_inj). In other processes, such as SA-SAGD or VAPEX, this assumption may be less accurate. Alternatively, the pressure distribution along the injector may be estimated, e.g. using the injection pressure and a frictional flow model along the injection well.

Typically, the changes in liquid level in the reservoir may be considered negligible directly following the well shut-in. For example, the liquid level may not change significantly within the first two days or so following a shut-in. FIG. 10 is a plot of local liquid level height (y-axis) as a function of reservoir pressure (x-axis) during a simulated SAGD operation using injector and producer wellbores spaced 5 m apart, where the liquid level was being held at about 2.5 m. The different plot lines represent values taken for different times during the simulated operational life (i.e. at 680 days of simulated operation, and at 1400 days, 2120 days, 2840 days, 3560 days, and (following a simulated shut-in) at 3602 days). Based on simulated results, the range of liquid level change over a 2 day shut-in may be on the order of 10% of the inter-well spacing distance.

At 835, a local shut-in subcool value is determined for each of the plurality of inflow zones. Preferably, the shut-in subcool value for an inflow zone is based on a local saturation temperature of an injection fluid at the measured shut-in pressure at that inflow zone, and the measured shut-in temperature at that inflow zone. For example, for a SAGD or SA-SAGD process, the local shut-in subcool value for an inflow zone may be defined as the difference between the saturation temperature T_sat for steam at the local shut-in pressure P_{res_inflow} at that zone (i.e. T_sat(P_{res_inflow})) and the local shut-in temperature T_{res_inflow} at that zone:Subcool_shut-ini=T_sat(P_{res_inflow(shut-in)i})−T_{res_inflow(shut-in)i}  (4)As discussed above, the local shut-in pressure in the reservoir adjacent the inflow location P_{res_inflow(shut-in)} may be assumed as being equal to a pressure value P_inflow measured by a pressure sensor 230, or may be based on a measured pressure value P_inflow subject to an adjustment factor (e.g. to compensate for a pressure drop across the reservoir/wellbore interface).

For a heated VAPEX (H-VAPEX) process, the local subcool value for an inflow zone may be defined as the difference between the saturation temperature T_sat for the solvent being used at the local shut-in pressure P_{res_inflow} at that zone and the local shut-in temperature T_{res_inflow} at that zone.

At 840, a local profile value is determined for each of the plurality of inflow zones. The local profile value S_T for each inflow zone is based on the local shut-in subcool value for that inflow zone and the local shut-in liquid level for that inflow zone:

$\begin{array}{cc}{S}_{T_i}=\frac{{\mathrm{Subcool}}_{\mathrm{shut}\text{-}{\mathrm{in}}_i}}{h_i}& \left(5\right)\end{array}$ Combining equations (4) and (5):

$\begin{array}{cc}{S}_{T_i}=\frac{T_{\mathrm{sat}}\left(P_{\mathrm{res}\_\mathrm{inflow}{\left(\mathrm{shut}\text{-}\mathrm{in}\right)}_i}\right)-T_{\mathrm{res}\_\mathrm{inflow}{\left(\mathrm{shut}\text{-}\mathrm{in}\right)}_i}}{h_i}& \left(6\right)\end{array}$ The local profile value S_Ti can be characterized as the change in subcool required to move the liquid level by one meter (presuming the liquid level h is measured in meters, otherwise unit conversion would be required).

For example, FIG. 11 illustrates an example plot of local profile values S_Ti from a simulated SAGD operation using injector and producer wellbores spaced 5 m apart, where the liquid level was being held at about 2.5 m. The different plot lines represent values taken for different times during the simulated operational life (i.e. at 680 days of simulated operation, and at 1400 days, 2120 days, 2840 days, 3560 days, and (following a simulated shut-in) at 3602 days). In this illustrative example, there is a generally linear relationship between local liquid level heights (y axis) and local subcool values (x-axis) for locations in the reservoir below the local liquid level. For locations in the reservoir above the local liquid level, the T_sat−T slope is approximately zero.

At 845, flow is resumed in the production wellbore and the injection wellbore. It will be appreciated that flow may be resumed prior to steps 830, 835, and/or 840, as these steps may be performed anytime using the measurements taken during shut-in.

At 850, a local operating temperature (i.e. a temperature measured during operating conditions after flow in the wellbores has resumed) for an inflow zone is measured using one or more temperature sensors distributed along the producer wellbore 200.

At 855, a local operating pressure (i.e. a pressure measured during operating conditions after flow in the wellbores has resumed) for the inflow zone is measured using one or more pressure sensors distributed along the producer wellbore 200.

At 860, a local operating subcool value is determined for the inflow zone. Like the shut-in subcool values determined at 835, the operating subcool value for an inflow zone is based on the measured operating temperature at that inflow zone. For example, for a SAGD or SA-SAGD process, the local operating subcool value for an inflow zone may be defined as the difference between the saturation temperature T_sat for steam at the local operating pressure P_inflow (or P_{res_inflow}) at that zone (i.e. T_sat(P_inflow)) and the local operating temperature T_inflow (or T_{res_inflow}) at that zone.Subcool_operatingi=T_sat(P_{res_inflow(operating)i})−T_{res_inflow(operating)i}  (7)

At 865, a local operating liquid level is determined for the inflow zone. The local operating liquid level may be determined by taking the difference between the local operating subcool value for the inflow zone and the local shut-in subcool value for the inflow zone (determined at 835). Next, this change in the local subcool value and the local profile value (determined at 840) can be used to determine a change in the local liquid level. This change in the local liquid level can be applied to the local shut-in liquid level for the inflow zone (determined at 830) to estimate the local operating liquid level. For example:

$\begin{array}{cc}{\mathrm{Subcool}}_{{\mathrm{delta}}_i}={\mathrm{Subcool}}_{{\mathrm{operating}}_i}-{\mathrm{Subcool}}_{\mathrm{shut}\text{-}{\mathrm{in}}_i}& \left(8\right)\\ h_{{\mathrm{delta}}_i}=\frac{{\mathrm{Subcool}}_{{\mathrm{delta}}_i}}{S_{T_i}}& \left(9\right)\\ h_{{\mathrm{operating}}_i}=h_{{\mathrm{delta}}_i}+h_{\mathrm{shut}\text{-}{\mathrm{in}}_i}& \left(10\right)\end{array}$

Alternatively, equations (10), (9), and (5) may be combined to express the local operating liquid level as a function of the local operating subcool value and the local profile value:

$\begin{array}{cc}{h}_{{\mathrm{operating}}_i}=\frac{{\mathrm{Subcool}}_{{\mathrm{operating}}_i}}{S_{T_i}}& \left(11\right)\end{array}$

Optionally, steps 810 to 840 may be performed each time the wellbores are shut-in (e.g. during scheduled service interruptions) to determine updated local liquid levels based on pressures measured during static flow conditions. An advantage of periodically re-determining the local shut-in liquid levels is that this may improve the accuracy of the liquid levels estimated during operation, as the re-determined baseline local liquid levels may be more accurate than local liquid levels estimated following a significant time period following the prior shut-in.

Additionally, or alternatively, steps 810 to 840 may be performed each time the wellbores are shut-in (e.g. during scheduled service interruptions) to determine updated local profile values. An advantage of periodically re-determining the profile values is that the relationship between a subcool change and a change in the local liquid level may ‘drift’ over time during the recovery process.

For example, FIG. 12 illustrates an example plot of a local profile value from a simulated SAGD operation using injector and producer wellbores spaced 5 m apart, where the liquid level was being held at about 2.5 m. In this example, the change in the local profile value (i.e. the slope of subcool/liquid level) (y-axis) as a function of operating time (x-axis) is generally monotonically increasing over the first 2,000 days or so, after which it may stabilize around a long-run value.

Preferably, after an updated local profile value is determined, the rate of ‘drift’ of the profile value (i.e. change in the local profile value as a function of operating time) may be estimated for the time period between the determination of the updated profile value and the prior profile value. This estimation of the ‘drift’ rate may be used as a factor during the liquid level determination at 865.

For example, the change in the local subcool value (i.e. the difference between the local operating subcool value for the inflow zone and the local shut-in subcool value for the inflow zone) may be scaled by an adjusted profile value (e.g. the local profile value determined at 840 scaled by the expected ‘drift’ rate for the time duration since the last shut-in) to determine a change in the local liquid level. This change in the local liquid level can then be applied to the local shut-in liquid level for the inflow zone (determined at 830) to estimate the local operating liquid level.

By determining (and preferably periodically updating) local profile values during shut-in conditions, local operating liquid levels for a number of locations distributed along the horizontal segment 106 of the injector wellbore may be determined using operating pressure and temperature data for these locations. This may allow for improved control of the liquid level between the injector and producer wellbores during a gravity drainage process (e.g. SAGD).

As discussed above, obtaining pressure and temperature data and determining local shut-in and operating state information for a number of locations distributed along the horizontal segments of the producer and/or injector wellbores may allow a more accurate and/or more detailed model to be developed for the production inflow and/or reservoir conditions along the wellbore. For such a model to allow for improved control of production during the SAGD process (e.g. by facilitating faster identification and/or responses to system changes), the local operating conditions are preferably updated in real-time or near-real time to provide current state information. Thus, one or more computing devices may be used to perform some or all of the calculations described herein. For example, it may be considered impractical (if not impossible) to determine and display, in a timely manner, an estimate of the liquid level h between the injector and producer at a number of locations along the wellbores without using one or more computing devices.

Also, updating such a model in real-time or near-real time to provide current state information may have one or more advantages. For example, such an updated model may facilitate improved steam conformance by adjusting heel/toe steam rates based on liquid level measurements.

For example, in response to determining that liquid levels are rising and/or above a target value, one or more actions may be taken promote the reduction of liquid levels. Non-limiting examples of such actions include: increasing the total flowrate for fluids exiting the wellbore segment (e.g. by increasing a pump rate of an artificial lift device); increasing an open area of at least one of the plurality of inflow locations, and; unblocking the open area of at least one of the plurality of inflow zones. During such actions, an injection rate may be raised to increase a total flow rate of fluids into the injector wellbore to maintain chamber pressure as the liquid level falls (e.g. the injection rate may be ‘ramped up’ temporarily, and then ‘dialed back’ to (approximately) the same rate once the liquid level has stabilized at a lower level), or the injection rate may be lowered, in order to decrease a total flow rate of fluids into the injector wellbore.

In response to determining that liquid levels are falling and/or below a target value, one or more actions may be taken promote an increase of liquid levels. Non-limiting examples of such actions include: decreasing the total flowrate for fluids exiting the wellbore segment (e.g. by decreasing a pump rate of an artificial lift device); decreasing an open area of at least one of the plurality of inflow locations, and; blocking the open area of at least one of the plurality of inflow zones. During such actions, an injection rate may be lowered to decrease a total flow rate of fluids into the injector wellbore to maintain chamber pressure as the liquid level rises (e.g. the injection rate may be ‘dialed back’ temporarily, and then ‘ramped up’ to (approximately) the same rate once the liquid level has stabilized at a higher level), or the injection rate may be raised, in order to increase a total flow rate of fluids into the injector wellbore.

It will be appreciated that other actions may be taken in response to high/rising or low/falling liquid levels. For example, in response to determining that liquid levels are rising and/or above a target value, an injection rate may be raised to increase a total flow rate of fluids into the injector wellbore, which may lead to lower or maintained liquid levels in the steam chamber, but only after a significant time delay. However, an increase in the injection rate may also result in an increase in the steam chamber temperature, which may increase the bitumen drainage rate in the steam chamber due to a reduction in bitumen viscosity. However, this impact may also have a significant time delay in that changes to the injection rate result in changes to the bitumen drainage rate at a time significantly delayed from the change in injection rate. Therefore, in embodiments herein, the control of the injection rate may have to be independently controlled (i.e., either increased or decreased) in any liquid level control situation, independent of the other liquid level control steps described herein.

Alternatively, or additionally, such an updated model may facilitate reducing gas vapor fractions in the producer, which in turn may reduce or preferably minimize pump failure and liner failures due to high velocity flows through the completions (e.g. possibly with sand moving with the high velocity fluid).

The various embodiments of the methods and systems described herein may be implemented using a combination of hardware and software. These embodiments may be implemented in part using computer programs executing on one or more programmable devices, each programmable device including at least one processor, an operating system, one or more data stores (including volatile memory or non-volatile memory or other data storage elements or a combination thereof), at least one communication interface and any other associated hardware and software that is necessary to implement the functionality of at least one of the embodiments described herein. For example, and without limitation, suitable computing devices may include one or more of a server, a network appliance, an embedded device, a personal computer, a laptop, a wireless device, or any other computing device capable of being configured to carry out some or all of the methods described herein.

In at least some of the embodiments described herein, program code may be applied to input data to perform at least some of the functions described herein and to generate output information. The output information may be applied to one or more output devices, for display or for further processing.

For example, a computer monitor or other display device may be configured to display a graphical representation of determined local liquid levels (under shut-in and/or operating conditions) for some or all of the inflow zones. In some embodiments, a schematic representation of the injector, producer, and formation (e.g. similar to FIGS. 2 to 7) may be displayed, along with a representation (e.g. a line, one or more line segments, or other symbols or indicia) of local liquid levels in the reservoir. For example, a representation of local liquid levels for all or some (e.g. 10%, 20%, or 50%) of the length between the heel and the toe of the wellbore segment may be displayed.

At least some of the embodiments described herein that use programs may be implemented in a high level procedural or object oriented programming and/or scripting language or both. Accordingly, the program code may be written in C, Java, SQL or any other suitable programming language and may comprise modules or classes, as is known to those skilled in object oriented programming. However, other programs may be implemented in assembly, machine language or firmware as needed. In either case, the language may be a compiled or interpreted language.

The computer programs may be stored on a storage media (e.g. a computer readable medium such as, but not limited to, ROM, magnetic disk, optical disc) or a device that is readable by a general or special purpose computing device. The program code, when read by the computing device, configures the computing device to operate in a new, specific, and predefined manner in order to perform at least one of the methods described herein.

As used herein, the wording “and/or” is intended to represent an inclusive-or. That is, “X and/or Y” is intended to mean X or Y or both, for example. As a further example, “X, Y, and/or Z” is intended to mean X or Y or Z or any combination thereof.

While the above description describes features of example embodiments, it will be appreciated that some features and/or functions of the described embodiments are susceptible to modification without departing from the spirit and principles of operation of the described embodiments. For example, the various characteristics which are described by means of the represented embodiments or examples may be selectively combined with each other. Accordingly, what has been described above is intended to be illustrative of the claimed concept and non-limiting. It will be understood by persons skilled in the art that other variants and modifications may be made without departing from the scope of the invention as defined in the claims appended hereto. The scope of the claims should not be limited by the preferred embodiments and examples, but should be given the broadest interpretation consistent with the description as a whole.

EMBODIMENTS

Embodiment 1

A method for determining a liquid level in a formation between a horizontal segment of an injection wellbore and a horizontal segment of a production wellbore, the method comprising:

• • shutting-in the production wellbore;
  • shutting-in the injection wellbore;
  • measuring, using at least one first temperature sensor positioned in the production wellbore segment, a local shut-in temperature for each of a plurality of inflow zones between a heel and a toe of the production wellbore segment;
  • measuring, using at least one first pressure sensor positioned in the production wellbore segment, a local shut-in pressure for each of the plurality of inflow zones;
  • determining, for each of the plurality of inflow zones:
    • a local shut-in liquid level, based on the measured shut-in pressure at that inflow zone and a shut-in pressure for an injection zone horizontally aligned with that inflow zone;
    • a local shut-in subcool value, based on the measured shut-in temperature at that inflow zone; and
    • a local profile value, based on the local shut-in subcool value for that inflow zone and the local shut-in liquid level for that inflow zone;
  • resuming flow in the production wellbore;
  • resuming flow in the injection wellbore;
  • after resuming flow in the production and injection wellbores, for at least one of the plurality of inflow zones:
    • measuring, using the at least one first temperature sensor positioned in the production wellbore, a local operating temperature for that inflow zone;
    • determining a local operating subcool value, based on the measured operating temperature at that inflow zone;
    • determining a local operating liquid level, based on the local operating subcool value for that inflow zone and the local profile value for that inflow zone.

Embodiment 2

The method of embodiment 1, wherein a local operating liquid level is determined for each of the plurality of inflow zones.

Embodiment 3

The method of embodiment 1 or embodiment 2, wherein the determined local shut-in subcool value is based on a local saturation temperature of an injection fluid at the measured shut-in pressure at that inflow zone and the measured shut-in temperature at that inflow zone.

Embodiment 4

The method of any one of embodiments 1 to 3, further comprising, after resuming flow in the production and injection wellbores, measuring, using the at least one first pressure sensor, a local operating pressure for that inflow zone, and wherein the determined local operating subcool value is based on a local saturation temperature of the injection fluid at the measured operating pressure at that inflow zone and the measured operating temperature at that inflow zone.

Embodiment 5

The method of any one of embodiments 1 to 4, wherein the determined local operating liquid level is based on the local shut-in liquid level for that inflow zone, a difference between the local operating subcool value for that inflow zone and the local shut-in subcool value for that inflow zone, and the local profile value for that inflow zone.

Embodiment 6

The method of any one of embodiments 1 to 5, wherein the local shut-in temperature for each of the plurality of injection zones is obtained using at least one second temperature sensor positioned in the injection wellbore.

Embodiment 7

The method of any one of embodiments 1 to 6, wherein the local shut-in pressure for each of the plurality of injection zones is obtained using at least one second pressure sensor positioned in the injection wellbore.

Embodiment 8

The method of any one of embodiments 1 to 7, further comprising:

• • after determining the local operating liquid level for the at least one of the plurality of inflow zones:
    • comparing the determined local operating liquid level for the at least one of the plurality of inflow zones to a target liquid level;
    • in response to the determined local operating liquid level for the at least one of the plurality of inflow zones being greater than the target liquid level, performing at least one of:
      • increasing a pump rate of an artificial lift device to increase the total flowrate for fluids exiting the production wellbore segment;
      • increasing an open area of at least one of the plurality of inflow zones; and
      • unblocking the open area of at least one of the plurality of inflow zones; and
    • in response to the target liquid level being greater than the determined local operating liquid level for the at least one of the plurality of production zones, performing at least one of:
      • decreasing the pump rate of the artificial lift device to decrease the total flowrate for fluids exiting the production wellbore segment;
      • decreasing the open area of at least one of the plurality of inflow zones; and
      • blocking the open area of at least one of the plurality of inflow zones.

Embodiment 9

The method of embodiment 8, wherein, in response to the determined local operating liquid level for at least one of the plurality of inflow zones being greater than the target liquid level, the method further comprises increasing an injection rate of a fluid injector to increase a total flow rate of fluids into the injector wellbore, in order to maintain pressure in a steam chamber.

Embodiment 10

The method of embodiment 8, wherein, in response to the determined local operating liquid level for at least one of the plurality of inflow zones being greater than the target liquid level, the method further comprises decreasing an injection rate of a fluid injector to decrease a total flow rate of fluids into the injector wellbore, in order to decrease a bitumen drainage rate in a steam chamber.

Embodiment 11

The method of embodiment 8, wherein, in response to the target liquid level being greater than the determined local operating liquid level for at least one of the plurality of inflow zones, the method further comprises decreasing an injection rate of a fluid injector to decrease a total flow rate of fluids into the injector wellbore, in order to maintain pressure in a steam chamber.

Embodiment 12

The method of embodiment 8, wherein, in response to the target liquid level being greater than the determined local operating liquid level for at least one of the plurality of inflow zones, the method further comprises increasing an injection rate of a fluid injector to increase a total flow rate of fluids into the injector wellbore, in order to increase a bitumen drainage rate in a steam chamber.

Embodiment 13

The method of any one of embodiments 1 to 12, further comprising, after determining the local operating liquid level for the at least one of the plurality of inflow zones:

• • shutting-in the production and injection wellbores a second time;
  • determining updated local profile values for each of the plurality of inflow zones;
  • resuming flow in the production and injection wellbores a second time;
  • after resuming flow in the production and injection wellbores the second time, for at least one of the plurality of inflow zones:
    • determining an updated local operating liquid level, based on an updated local shut-in liquid level for that inflow zone, a difference between an updated local operating subcool value for that inflow zone and an updated local shut-in subcool value for that inflow zone, and the updated local profile value for that inflow zone.

Embodiment 14

The method of any one of embodiments 1 to 12, further comprising:

• • after determining the local profile values during a first shut-in period:
    • determining updated local profile values during a second shut-in period;
    • determining, for at least one of the plurality of inflow zones, a profile adjustment factor based on the local profile value for that inflow zone, the updated local profile value for that inflow zone, and a duration between the first and second shut-in periods; and
  • after resuming flow in the production and injection wellbores following the second shut-in period, for at least one of the plurality of inflow zones:
    • determining a local operating liquid level, based on the local shut-in liquid level for that inflow zone, a difference between the local operating subcool value for that inflow zone and the local shut-in subcool value for that inflow zone, the updated local profile value for that inflow zone, the local profile adjustment factor for that inflow zone, and a duration between the second shut-in period and a period during which the local operating temperature and pressure were measured when determining the subcool value for that inflow zone.

Embodiment 15

The method of any one of embodiments 1 to 14, further comprising:

• • after shutting in the injection wellbore, and before determining the local shut-in liquid levels:
    • performing a gas purge of the injector wellbore.

Embodiment 16

A system for determining a liquid level in a formation between a horizontal segment of an injection wellbore and a horizontal segment of a production wellbore, the system comprising:

• • at least one first temperature sensor positioned in the production wellbore segment to measure a local temperature for each of a plurality of inflow zones between a heel and a toe of the production wellbore segment;
  • at least one first pressure sensor positioned in the production wellbore segment to measure a local pressure for each of the plurality of inflow zones;
  • one or more processors operatively coupled to the at least one first temperature sensor and the at least one first pressure sensor, the one or more processors, collectively, configured to:
    • during a period in which the production wellbore and the injection wellbore are shut-in:
      • determine, for each of the plurality of inflow zones:
        • a local shut-in liquid level, based on a measured shut-in pressure at that inflow zone and a shut-in pressure for an injection zone horizontally aligned with that inflow zone;
        • a local shut-in subcool value, based on a measured shut-in temperature at that inflow zone; and
        • a local profile value, based on the local shut-in subcool value for that inflow zone and the local shut-in liquid level for that inflow zone; and
    • after resuming flow in the production and injection wellbores:
      • determine, for at least one of the plurality of inflow zones:
        • a local operating subcool value, based on a measured operating temperature at that inflow zone; and
        • a local operating liquid level, based on the local operating subcool value for that inflow zone and the local profile value for that inflow zone.

Embodiment 17

The system of embodiment 16, wherein the one or more processors are configured to determine the local shut-in subcool value for each of the plurality of inflow zones based on the measured shut-in temperature at that inflow zone and a local saturation temperature of an injection fluid at the measured shut-in pressure at that inflow zone.

Embodiment 18

The system of embodiment 16 or embodiment 17, wherein the one or more processors are configured to determine the local operating subcool value for the at least one of the plurality of inflow zones based on the measured operating temperature at that inflow zone and a local saturation temperature of the injection fluid at a measured operating pressure at that inflow zone.

Embodiment 19

The system of any one of embodiments 16 to 18, wherein the one or more processors are configured to determine the local operating liquid level based on the local shut-in liquid level for that inflow zone, a difference between the local operating subcool value for that inflow zone and the local shut-in subcool value for that inflow zone, and the local profile value for that inflow zone.

Embodiment 20

The system of any one of embodiments 16 to 19, wherein the at least one first temperature sensor comprises a thermocouple or a set of thermocouples.

Embodiment 21

The system of any one of embodiments 16 to 19, wherein the at least one first temperature sensor comprises a distributed temperature sensor (DTS).

Embodiment 22

The system of embodiment 20 or embodiment 21, further comprising at least one second temperature sensor positioned in the injection wellbore to measure a local temperature for each of a plurality of injection zones between a heel and a toe of the injection wellbore segment.

Embodiment 23

The system of any one of embodiments 16 to 22, wherein the at least one first pressure sensor comprises a distributed pressure sensing system.

Embodiment 24

The system of any one of embodiments 16 to 23, wherein the at least one first pressure sensor is positioned exterior of a production string located in the production wellbore segment.

Embodiment 25

The system of any one of embodiments 16 to 24, wherein the at least one first pressure sensor comprises fewer discrete pressure sensors than the number of inflow zones in the plurality of inflow zones, and wherein, for inflow zones without a discrete pressure sensor positioned therein, the one or more processors are configured to determine local pressures for those inflow zones using a model based on pressures from discrete pressure sensors positioned in other inflow zones.

Embodiment 26

The system of any one of embodiments 16 to 25, further comprising at least one second pressure sensor positioned in the injection wellbore to measure a local pressure for each of the plurality of injection zones.

Embodiment 27

The system of embodiment 26, wherein the at least one second pressure sensor comprises fewer discrete pressure sensors than the number of injection zones in the plurality of injection zones, and wherein, for injection zones without a discrete pressure sensor positioned therein, the one or more processors are configured to determine local pressures for those injection zones using a model based on pressures from discrete pressure sensors positioned in other injection zones.

Embodiment 28

The system of any one of embodiments 16 to 27, wherein the plurality of inflow zones comprises at least five inflow zones.

Embodiment 29

The system of any one of embodiments 16 to 28, further comprising a display device operatively coupled to the one or more processors, and wherein the one or more processors are further configured to cause the display device to display a graphical representation of the determined local operating liquid levels for the at least one of the plurality of inflow zones.

Embodiment 30

The system of embodiment 29, wherein the graphical representation of the determined local operating liquid levels for the at least one of the plurality of inflow zones comprises a representation of local operating liquid levels for at least ten percent of a length between the heel and the toe of the production wellbore segment.

Claims

1. A method for determining a liquid level in a formation between a horizontal segment of an injection wellbore and a horizontal segment of a production wellbore, the method comprising: shutting-in the production wellbore;shutting-in the injection wellbore;measuring, using at least one first temperature sensor positioned in the production wellbore segment, a local shut-in temperature for each of a plurality of inflow zones between a heel and a toe of the production wellbore segment;measuring, using at least one first pressure sensor positioned in the production wellbore segment, a local shut-in pressure for each of the plurality of inflow zones;determining, for each of the plurality of inflow zones: a local shut-in liquid level, based on the measured shut-in pressure at that inflow zone and a shut-in pressure for an injection zone horizontally aligned with that inflow zone;a local shut-in subcool value, based on the measured shut-in temperature at that inflow zone; anda local profile value, based on the local shut-in subcool value for that inflow zone and the local shut-in liquid level for that inflow zone, the local profile value being a relationship between a change of the local shut-in subcool value and a change of the local shut-in liquid level;resuming flow in the production wellbore;resuming flow in the injection wellbore;after resuming flow in the production and injection wellbores, for at least one of the plurality of inflow zones: measuring, using the at least one first temperature sensor positioned in the production wellbore, a local operating temperature for that inflow zone;determining a local operating subcool value, based on the measured operating temperature at that inflow zone;determining a local operating liquid level, based on the local operating subcool value for that inflow zone and the local profile value for that inflow zone.

2. The method of claim 1, wherein a local operating liquid level is determined for each of the plurality of inflow zones.

3. The method of claim 1, wherein the determined local shut-in subcool value is based on a local saturation temperature of an injection fluid at the measured shut-in pressure at that inflow zone and the measured shut-in temperature at that inflow zone.

4. The method of claim 1, further comprising, after resuming flow in the production and injection wellbores, measuring, using the at least one first pressure sensor, a local operating pressure for that inflow zone, and wherein the determined local operating subcool value is based on a local saturation temperature of the injection fluid at the measured operating pressure at that inflow zone and the measured operating temperature at that inflow zone.

5. The method of claim 1, wherein the determined local operating liquid level is based on the local shut-in liquid level for that inflow zone, a difference between the local operating subcool value for that inflow zone and the local shut-in subcool value for that inflow zone, and the local profile value for that inflow zone.

6. The method of claim 1, wherein the local shut-in temperature for each of the plurality of injection zones is obtained using at least one second temperature sensor positioned in the injection wellbore.

7. The method of claim 1, wherein the local shut-in pressure for each of the plurality of injection zones is obtained using at least one second pressure sensor positioned in the injection wellbore.

8. The method of claim 1, further comprising: after determining the local operating liquid level for the at least one of the plurality of inflow zones: comparing the determined local operating liquid level for the at least one of the plurality of inflow zones to a target liquid level;in response to the determined local operating liquid level for the at least one of the plurality of inflow zones being greater than the target liquid level, performing at least one of: increasing a pump rate of an artificial lift device to increase the total flowrate for fluids exiting the production wellbore segment;increasing an open area of at least one of the plurality of inflow zones; andunblocking the open area of at least one of the plurality of inflow zones; andin response to the target liquid level being greater than the determined local operating liquid level for the at least one of the plurality of production zones, performing at least one of: decreasing the pump rate of the artificial lift device to decrease the total flowrate for fluids exiting the production wellbore segment;decreasing the open area of at least one of the plurality of inflow zones; andblocking the open area of at least one of the plurality of inflow zones.

9. The method of claim 8, wherein, in response to the determined local operating liquid level for at least one of the plurality of inflow zones being greater than the target liquid level, the method further comprises increasing an injection rate of a fluid injector to increase a total flow rate of fluids into the injector wellbore, in order to maintain pressure in a steam chamber.

10. The method of claim 8, wherein, in response to the determined local operating liquid level for at least one of the plurality of inflow zones being greater than the target liquid level, the method further comprises decreasing an injection rate of a fluid injector to decrease a total flow rate of fluids into the injector wellbore, in order to decrease a bitumen drainage rate in a steam chamber.

11. The method of claim 8, wherein, in response to the target liquid level being greater than the determined local operating liquid level for at least one of the plurality of inflow zones, the method further comprises decreasing an injection rate of a fluid injector to decrease a total flow rate of fluids into the injector wellbore, in order to maintain pressure in a steam chamber.

12. The method of claim 8, wherein, in response to the target liquid level being greater than the determined local operating liquid level for at least one of the plurality of inflow zones, the method further comprises increasing an injection rate of a fluid injector to increase a total flow rate of fluids into the injector wellbore, in order to increase a bitumen drainage rate in a steam chamber.

13. The method of claim 1, further comprising, after determining the local operating liquid level for the at least one of the plurality of inflow zones: shutting-in the production and injection wellbores a second time;determining updated local profile values for each of the plurality of inflow zones;resuming flow in the production and injection wellbores a second time;after resuming flow in the production and injection wellbores the second time, for at least one of the plurality of inflow zones: determining an updated local operating liquid level, based on an updated local shut-in liquid level for that inflow zone, a difference between an updated local operating subcool value for that inflow zone and an updated local shut-in subcool value for that inflow zone, and the updated local profile value for that inflow zone.

14. The method of claim 1, further comprising: after determining the local profile values during a first shut-in period: determining updated profile values during a second shut-in period;determining, for at least one of the plurality of inflow zones, a profile adjustment factor based on the local profile value for that inflow zone, the updated local profile value for that inflow zone, and a duration between the first and second shut-in periods; andafter resuming flow in the production and injection wellbores following the second shut-in period, for at least one of the plurality of inflow zones: determining a local operating liquid level, based on the local shut-in liquid level for that inflow zone, a difference between the local operating subcool value for that inflow zone and the local shut-in subcool value for that inflow zone, the updated profile value for that inflow zone, the profile adjustment factor for that inflow zone, and a duration between the second shut-in period and a period during which the local operating temperature and pressure were measured when determining the subcool value for that inflow zone.

15. The method of claim 1, further comprising: after shutting in the injection wellbore, and before determining the local shut-in liquid levels: performing a gas purge of the injector wellbore.

16. A system for determining a liquid level in a formation between a horizontal segment of an injection wellbore and a horizontal segment of a production wellbore, the system comprising: at least one first temperature sensor positioned in the production wellbore segment to measure a local temperature for each of a plurality of inflow zones between a heel and a toe of the production wellbore segment;at least one first pressure sensor positioned in the production wellbore segment to measure a local pressure for each of the plurality of inflow zones;one or more processors operatively coupled to the at least one first temperature sensor and the at least one first pressure sensor, the one or more processors, collectively, configured to: during a period in which the production wellbore and the injection wellbore are shut-in: determine, for each of the plurality of inflow zones: a local shut-in liquid level, based on a measured shut-in pressure at that inflow zone and a shut-in pressure for an injection zone horizontally aligned with that inflow zone;a local shut-in subcool value, based on a measured shut-in temperature at that inflow zone; anda local profile value, based on the local shut-in subcool value for that inflow zone and the local shut-in liquid level for that inflow zone, the local profile value being a relationship between a change of the local shut-in subcool value and a change of the local shut-in liquid level; andafter resuming flow in the production and injection wellbores: determine, for at least one of the plurality of inflow zones: a local operating subcool value, based on a measured operating temperature at that inflow zone; anda local operating liquid level, based on the local operating subcool value for that inflow zone and the local profile value for that inflow zone.

17. The system of claim 16, wherein the one or more processors are configured to determine the local shut-in subcool value for each of the plurality of inflow zones based on the measured shut-in temperature at that inflow zone and a local saturation temperature of an injection fluid at the measured shut-in pressure at that inflow zone.

18. The system of claim 16, wherein the one or more processors are configured to determine the local operating subcool value for the at least one of the plurality of inflow zones based on the measured operating temperature at that inflow zone and a local saturation temperature of the injection fluid at a measured operating pressure at that inflow zone.

19. The system of claim 16, wherein the one or more processors are configured to determine the local operating liquid level based on the local shut-in liquid level for that inflow zone, a difference between the local operating subcool value for that inflow zone and the local shut-in subcool value for that inflow zone, and the local profile value for that inflow zone.

20. The system of claim 16, wherein the at least one first temperature sensor comprises at least one of a distributed temperature sensor (DTS) and a thermocouple or a set of thermocouples.

21. The system of claim 16, further comprising at least one second temperature sensor positioned in the injection wellbore to measure a local temperature for each of a plurality of injection zones between a heel and a toe of the injection wellbore segment.

22. The system of claim 16, wherein the at least one first pressure sensor comprises a distributed pressure sensing system.

23. The system of claim 16, wherein the at least one first pressure sensor is positioned exterior of a production string located in the production wellbore segment.

24. The system of claim 16, wherein the at least one first pressure sensor comprises fewer discrete pressure sensors than the number of inflow zones in the plurality of inflow zones, and wherein, for inflow zones without a discrete pressure sensor positioned therein, the one or more processors are configured to determine local pressures for those inflow zones using a model based on pressures from discrete pressure sensors positioned in other inflow zones.

25. The system of claim 16, further comprising at least one second pressure sensor positioned in the injection wellbore to measure a local pressure for each of the plurality of injection zones.

26. The system of claim 24, wherein the at least one second pressure sensor comprises fewer discrete pressure sensors than the number of injection zones in the plurality of injection zones, and wherein, for injection zones without a discrete pressure sensor positioned therein, the one or more processors are configured to determine local pressures for those injection zones using a model based on pressures from discrete pressure sensors positioned in other injection zones.

27. The system of claim 16, wherein the plurality of inflow zones comprises at least five inflow zones.

28. The system of claim 16, further comprising a display device operatively coupled to the one or more processors, and wherein the one or more processors are further configured to cause the display device to display a graphical representation of the determined local operating liquid levels for the at least one of the plurality of inflow zones.