Field-scale investigation of different miscible

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Field-scale investigation of different miscible CO2-injection modes to improve oil recovery in a clastic highly heterogeneous reservoir

Ahmed Khalil Jaber1 Mariyamni B. Awang2

Received: 19 January 2016 / Accepted: 22 May 2016 / Published online: 11 June 2016 The Author(s) 2016. This article is published with open access at Springerlink.com

Abstract Carbon dioxide ooding is considered one of the most commonly used miscible gas injections to improve oil recovery, and its applicability has grown signicantly due to its availability, greenhouse effect and easy achievement of miscibility relative to other gases. Therefore, miscible CO2-injection is considered one of the most feasible methods worldwide. For long-term strategies in Iraq and the Middle East, most oilelds will need to improve oil recovery as oil reserves are falling. This paper presents a study of the effect of various CO2-injection modes on miscible ood performance of the highly heterogeneous clastic reservoir. An integrated eld-scale reservoir simulation model of miscible ooding is accomplished for this purpose. The compositional simulator, Eclipse compositional, has been used to investigate the feasibility of applying different miscible CO2-injection modes. The process of the CO2-injection was optimized to start in January 2056 as an improved oil recovery method after natural depletion and waterooding processes have been performed, and it will continue to January 2072. The minimum miscibility pressure was determined using empirical correlations as a function of reservoir crude oil composition and its properties. Four miscible CO2-injection modes were undertaken to investigate the reservoir performance. These modes were, namely the continuous CO2-injection (CCO2), water-alternating-CO2-injection (CO2-WAG), hybrid CO2-WAG injection, and

simultaneous water and CO2-injection (CO2-SWAG) processes. All injection modes were analyzed in respect to the net present value (NPV) and net present value index (NPVI) calculations to conrm the more feasible CO2 development strategy. The results indicated that the application of CO2-SWAG injection mode of 2:1 SWAG ratio attained the highest oil recovery, NPV and NPVI, among the other modes. The achieved incremental oil recovery by this process was 9.174 %, that is 189 MM STB of the oil produced higher than the waterooding case,1.113 % (23 MMSTB of oil) in comparison with the CCO2-ooding case, 1.176 % (24.3 MMSTB of oil) in comparison with the hybrid CO2-WAG case and almost0.987 % (204 MMSTB of oil) when compared with the CO2-WAG case. The results indicated that the application of CO2-WAG injection mode of 1.5:1 WAG ratio attained the highest oil recovery after the SWAG process.

Keywords CO2-injection Clastic heterogeneous reservoir

Field-scale analysis

List of symbolsNPV Net present value, USDNPVI Net present value indexCNPV Cumulative net present value, USDMCO Maximum capital outlay, minimum value on the cumulative NPV curve, USDFOE Field recovery factor, fractionFOPT Field oil production total, STBFOPR Field oil production rate, STB/dayFWCT Field watercut total, fractionFPR Field pressure, psiaCAPEX Capital expenditure, USDOPEX Operational expenditure, USD

& Ahmed Khalil Jaber [email protected]

1 Iraqi Ministry of Oil & Universiti Teknologi PETRONAS,31750 Tronoh, Perak, Malaysia

2 Universiti Teknologi PETRONAS, 31750 Tronoh, Perak, Malaysia

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NCF Net cash ow, USDt Future time, yearT Cumulative investment (or production) periodi Interest rate, fractionQw Water injection rate, STB/day

QCO2 CO2-injection rate, Scf/dayBCO2 CO2 formation volume factor, rbbl/Scf

Bw Water formation volume factor, rbbl/STB WACO2ratio Water-alternating-CO2 ratio

Nca Capillary numbert Velocity of the displacing phasel Viscosity of the displacing phaser Interfacial tension between oil and waterh Contact angle between oilwater interface and the rock surfacePc Capillary pressure, psi

Sw Water saturationSwn Normalized water saturation

Krwn Normalized water relative permeability Kron Normalized oil relative permeability nw Water exponent parameterno Oil exponent parameter

Introduction

CO2-ooding appeared in the 1930s and had great development in the 1970s (Hao et al. 2004). With over 40 years of production practice, CO2-ooding has become a leading

EOR technique for light and medium oils (Reid and David 1997). CO2-ooding is benecial for both the environment and the petroleum industry by injecting the harmful CO2 to increase oil recovery. This reduces greenhouse gas emissions by sequestration of CO2 in the reservoir, thus reducing heat trapped in the atmosphere. CO2-injection has been proved as a successful technology worldwide, with less minimum miscibility pressure than nitrogen and hydrocarbon gases. The studied reservoir was the Nahr Umr reservoir which is considered one of the most important producing reservoirs in the south of Iraq. This reservoir as with many of the southern Iraqi elds needs to apply improved oil recovery methods (IOR) in the nearest future to extract more oil and increase oil recovery. It is very necessary to screen, investigate and optimize the proper IOR method. IOR technology using CO2-injection has been proven to be more protable during recent years.

CO2-injection has a great potential of enhancing and increasing oil recovery. However, it does not recover all the oil, regardless of whether the reservoir has been previously ooded with water. Typically, recovery addition with miscible CO2 displacement is around 1020 %, by

injecting an equivalent of 80 % HCPV with CO2 (Marylena 2005).

The heterogeneity index for the Nahr Umr reservoir in the Subba oileld was determined based on Lorenz coefcient calculations. This was based on the ow capacity distribution to measure the contrast in the permeability relative to the homogeneous case (Ganesh and Satter 1994). The average Lorenz coefcient value for different core samples of the Nahr Umr reservoir was found equal to0.814, which indicates that this reservoir is a highly heterogeneous reservoir. The Subba oileld has a short history, as the experimental period during the 1990s. The production of the eld did not last due to some technical issues at that time. The reservoir heterogeneity measurements vary depending on the scale of the measurement. Webber and Van Geuns (1990) discovered that the geological heterogeneity also varies depending on the scale of the measurement. The reservoir heterogeneity has a signicant impact on uid ow. It is, therefore, crucial to investigate the CO2-ooding behavior with the eld-scale heterogeneity model. This model is able to incorporate all the reservoir heterogeneity. Most of the CO2 studies have been investigated with small-scale experimental core measurements. It is difcult to incorporate the reservoir heterogeneity into the small-scale measurements (Webber and Van Geuns 1990). There have been few works on CO2-ooding in small-scale heterogeneity carried out (Bennion and Bachu 2006). One of the signicant features of the current study is the effect of the full-eld-scale heterogeneity on oil recovery and sweep efciency across a heterogeneous model during CO2-ooding.

Due to the reservoirs heterogeneity, the optimal locations and number of inll wells were optimized based on sweet spots determined by dynamic opportunity index analyses (Al-Khazraji and Shuker 2015b). There were 50 inll wells and, accordingly, 21 injectors were decided to be involved in the development scenarios. The water-ooding process has been optimized to start up in January 2028 and will continue till January 2056 with 3000 bbl/day as the water injection rate for each well. The CO2-injection is proposed to commence in January 2056 as an IOR method after the waterooding process and will be tested till January 2072. In this study, four production strategies with different sensitivities under miscible CO2 were examined to optimize the best long-term miscible ooding strategy for the reservoir. These strategies include CCO2-injection with different slug sizes, CO2-WAG with different half-cycle rates, CO2-SWAG and hybrid CO2-WAG injection with different slug sizes. The compositional ow simulation model, Eclipse compositional, was used to construct the ow simulation runs. Eclipse compositional allowed the researcher to model a multicomponent hydro-carbon ow in order to get a detailed description of the

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phase behavior and compositional changes, and it used a cubic equation of state (EOS). The obtained results were analyzed depending on the NPV and NPVI analysis of the produced oil that were conducted for each case.

Background

The CO2-ooding process can be classied as miscible and immiscible. In the immiscible ooding process, the relatively high reservoir pressure results in the CO2 dissolution, oil viscosity reduction, lowering of interfacial tension, oil swelling and dissolved gas drive. In the miscible ooding mechanism, the process involves the generation of the miscibility at the minimum miscible pressure between the CO2 and reservoir oil, lowering the interfacial tension between the oil and CO2, and swelling of the oil due to the transferring of the CO2 into the oil, then, lowering the oil viscosity and density, and nally the increasing oil recovery factor. The miscibility between the CO2 and crude oil was achieved through the multiple contact miscibility process. CO2 was, rst condensed into the crude oil (transferring of CO2 to the oil), making oil lighter. The lighter components of the oil vaporized or were extracted by the reminder of the CO2, making the CO2 denser with a higher viscosity. The formed CO2 is called the rich phase;

as the mass transfer continued between the CO2 and oil, the formed CO2 became more like oil in terms of uid properties. The relative permeability of the gas (displacing phase) was reduced, and the mobility ratio was reduced. The capillary number increased, microscopic displacement efciency increased, and then the recovery factor was increased. The capillary number was dened by the following equation.

Nca

Viscouse Forces Capillary Forces

tlr cos h 1

where t and l are the velocity and the viscosity of the displacing phase, respectively, r is the interfacial tension between the oil and water and h is the contact angle between the oilwater interface and the rock surface measured between the rock surface and the denser phase. This takes place because the purpose of any EOR method is to increase the capillary number that leads to a favorable mobility ratio (M \ 1.0).

Using CO2 as the miscible gas injection is considered one of the more successfully enhanced oil recovery methods worldwide. The major factor affecting implementing the CO2-ooding is the economic criteria, i.e., its availability at an economical price (Mohamed et al. 2012). The net utilization ratio of CO2 per barrel of additional oil recovered varies from eld to eld, but on average has been estimated at 5.5 MSCF

CO2 per additional barrel of oil in the USA EOR overview

study by Broome et al. (1986) and between 4 and 6 MSCF/ barrel by a more recent study by Jeschke et al. (2000). In the USA, about 20 % of the total EOR production was obtained by CO2-ooding in 1992 (Ganesh and Satter 1994).

A comparison of EOR surveys (Rao et al. 2004; Kulkarni and Rao 2004) from 1971 to 2004 showed a signicant increase in the petroleum industry trend toward miscible gas injection EOR. The miscible gas injection accounts for nearly 80 % of the gas injection EOR (Kulkarni and Rao 2004). The CO2 share of the gas injection EOR oil increased from 39 % in 1984 to 65 % in 2004 (Rao et al. 2004;

Kulkarni and Rao 2004). Generally, CO2-injection can prolong the reservoir life for 1520 years and may recover an additional 1520 % of the original oil in place (Hao et al. 2004); this is mainly due to a higher microscopic displacement efciency of the CO2-ooding (Chen et al.

2009). However, CO2-ooding suffers from poor macroscopic displacement efciency in a heterogeneous reservoir due to the low viscosity of CO2. This leads to early a CO2 breakthrough, unstable pressure distribution, viscous ngering, channeling and bypass oil resulting in reduced oil recoveries. Therefore, the WAG technique process was proposed to improve the sweeping efciency of injected gas, control the mobility of the gas and stabilize the displacement front since the WAG technique combines the improved microscopic displacement efciency by gas with improved macroscopic displacement efciency by water. The WAG ooding process was rst applied in 1957 in Canada and reported in the literature by Caudle and Dyes in 1957. In recent years, the WAG process has gained an increasing interest for EOR in the USA; approximately 55 % of the total oil productions employing EOR methods are a result of gas injection methods, the majority of which are WAG processes. The literature review suggests that almost 80 % of the gas injection processes employ the WAG ooding process (Mohamed et al. 2012).

Many studies suggested that the CO2-WAG ooding process has usually been applied as a tertiary recovery method of ooding (Christensen et al. 1998; Babadagli 2005; Hadlow 2004). In contrast, many other studies indicated that the application of the WAG process in the early stages of the reservoir life produces an outcome of higher oil recovery with less pore volume being injected (Mahnaz and Farouq 1984; Shyeh-Yung 1991; Thomas and Leiv 2002; Mohamed et al. 2012; Behrouz and Ghazanfari 2004). Kulkarni and Rao (2005) indicated in their experimental work that the secondary mode miscible coreoods demonstrated high oil recoveries. Several CO2-ooding methods that have been used for EOR include:

1. Continuous CO2-injection (CCO2),2. Injection of water and CO2, simultaneously (CO2-SWAG),

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3. Injection of CO2 and water, alternately (CO2-WAG);4. Hybrid CO2-WAG injection process in which a large volume of gas is initially injected, followed by a number of small slugs of water and gas being injected (Christensen et al. 1998).

Research objectives

The main objective of the current study has been to investigate different modes of miscible CO2-ooding performance in a highly heterogeneous reservoir through a full-eld-scale analysis. Four modes of miscible CO2-ooding were examined for future reservoir performance prediction. These modes included the CCO2-injection, CO2-WAG, simultaneous water and CO2-injection (CO2-SWAG) and hybrid CO2-WAG injection techniques.

To achieve the objectives of this study, the following tasks had to be fullled:

1. Determining the optimum continuous CO2-injection rate.

2. Determining the optimum injection CO2-WAG ratio.3. Determining the optimum CO2-WAG half-cycle length.

4. Determining the optimum CO2-injection rate for the CO2-SWAG process.

5. Determining the optimum CO2-SWAG ratio.6. Determining the optimum CO2 slug size for the hybrid CO2-WAG process.

Methodology

In order to accomplish the aforementioned objectives, the following steps had to be followed:

1. Building the petrophysical study of the reservoir by employing Interactive Petrophysics (IP) software from Senergy Ltd.

2. Generating a PVT model of the reservoir by employing the PengRobinson cubic EOS by using Petroleum Expert PVTP software.

3. Building a 3D static geological model by employing Schlumberger Petrel software.

4. Generating a compositional simulation ow model through utilizing Eclipse compositional in order to demonstrate the effect of the miscible CO2-ooding process for improving oil recovery.

Reservoir characterization and description

The Subba oileld is located in the Southeast of Iraq, some110 km to the Northwest of Basra and 12 km Northwest of the Luhais oileld. The Subba oileld is described as a giant oileld with bottom and edge water support. There were 14 wells drilled in this eld which penetrated the Nahr Umr formation; but, only six of them were completed in the Nahr Umr reservoir.

The dimensions of the Subba oileld are about 30 km long and 7 km wide. The Nahr Umr reservoir is considered one of the most important productive reservoirs in the Southern Iraqi elds, which comprises an important place in the stratigraphic column of the Lower Cretaceous Albian Nahr Umr. It has a double dome separated by a shallow saddle. The largest one is located in the South of the eld and the smallest one in the North of the eld. This eld has not been developed for over the last 40 years, since it was produced in 1990 for a short experimental period from the Nahr Umr reservoir.

Static model

The purpose of the geological interpretation is to generate a robust 3D geological facies model of the Nahr Umr clastic reservoir in order to capture the lateral and vertical reservoir heterogeneity. The heterogeneity of the reservoir is dependent on the depositional environments and subsequent events (Ahmed 2010). The goal of reservoir characterization for heterogeneous formations is to establish a reservoir model based on explicitly modeling the known heterogeneities (conditioning to well observations) and using mathematical and geostatistical algorithms to systematically simulate the spatial distribution of the reservoir properties at inter-well locations. The modeled area was about 787 km2.

The Nahr Umr formation comprises a lower Cretaceous Albian clastic unit. This unit characterized by massive clean sands, which are overlain by a mixture of shale, silt and massive clean sand interbedded with shale. The formation is composed generally of interbedded black shale with coarse- to ne-grained sandstone (Aqrawi et al. 2010). The Nahr Umr formation in the South of Iraq is interpreted to be an alluvial to lower coastal plain to a deltaic deposit with shallow marine and aolian inuences (Aqrawi et al. 2010). The crest of the structure in the Subba oil eld occurs at a depth of (-2403) m SSTVD. The average thickness of the reservoir is about 195 m. The average pay thickness of the reservoir is about 26 m.

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The Nahr Umr reservoir in the Subba oil eld has been described from core photographs and a core description of 500 meters of the reservoir in the eld through seven wells. The core data and description have been integrated with a wireline log response to aid in the development of the geological model and in facies and reservoir quality predictions. There were four major facies groups were identied from the core photo description. These facies include sand uvial, sand tidal for the reservoir, siltstone and shale for the nonreservoir. Accurate high-resolution model is critical to have a better understanding of the reservoir heterogeneity for enhanced oil recovery. The geological model of the Nahr Umr formation has been constructed by utilizing Schlumbergers Petrel software in order to incorporate all available structural, logs and facies data.

The static model was constructed based on the petro-physical interpretation results (Al-Khazraji and Shuker 2014a, b, 2015a, b), structural contour maps of the formation geological layers and data from 14 wells penetrating the reservoir. These data comprised well coordinates, formation tops, core data, log interpretation results, facies and permeability curves (Al-Khazraji and Shuker 2014b; Well logs for Nahr Umr formationSubba oileld 19731980; nal well reports for Nahr Umr formation Subba oileld 19761990; nal geological reports for Nahr Umr formationSubba oileld, 19761990; core measurements reports for Nahr Umr formationSubba oileld 19761980; geological study for Subba oileld 2001). The log interpretation results included shale volume, porosity and water saturation. The petrophysical properties distribution, such as permeability, porosity and saturation, was constructed based on the facies model. The resultant 3D cellular model formed the basis for the reservoir simulation model that was used to optimize the reservoir development scenarios. The Nahr Umr reservoir has a heterogeneous permeability prole, including very high permeability for sandstone and very low permeability for shale.

Structural modeling

The model cells were dened as 200 m 9 200 m in the X-and Y-directions with 36 cell layers deep. The model was constructed of 36 cell layers deep, with the layer thickness differing and ranging as follows: 2.81 m for layers (18),12.28 m for layers (912), 3.91 for layers (1324) and 8.52 for layers (2536). This size of cells was efcient to capture the reservoir characteristic and the reservoir petro-physical property changes as well as to ensure that the derived geological grids could be exported into the simulation model directly, hence avoiding grid upscaling. The number of layers in the geological model was adjusted to ensure the match between the upscaled and well facies.

Then, a better denition was set for discrete ow units and the boundaries that separated the ow units in the reservoir.

The total number of cells considered in the geological model was set to 101 and 196 in the X-direction and Y-direction, respectively, considering 36 cells in the Z-direction. The total number of cells in the geological model became 712656 cells.

Petrophysical modeling

The generated heterogeneous distribution for porosity and permeability was matched with core laboratory measurements. The petrophysical derived log properties, porosity, permeability and water saturation, were scaled up into the cellular model. The scale up of the well logs was an automatic process with some user settings available. When scaling up the well logs Petrel software will rst nd the 3D grid cells that the wells penetrate. For each grid cell, all log values that fall within the cell will be averaged according to the selected algorithm to produce one log value for that cell (Petrel Seismic-to-Simulation software manual 2013). The petrophysical properties are modeled stochastically using the sequential Gaussian simulation (SGS) method, allowing for ner-scale heterogeneity and greater control as well as prediction of the petrophysical properties in areas away from the well data points. It assumes that the data to be modeled would have a Gaussian distribution from the upscaled logs.

Original oil in place (OOIP)

The volume of oil originally in places calculations was very important before embarking to reservoir performance prediction. The deterministic approach of the volumetric method was used in the original oil in place (OOIP) estimating for the reservoir, based on geological modeling calculations. The OOIP resulting from the geological modeling was basically consistent with that resulting from the volumetric method. The value of the initial oil formation volume factor (Boi) considered in the OOIP calculations was established from the PVT data at the initial pressure and was found to be equal to (1.18191 rbbl/STB). The estimated OOIP of the reservoir calculated from the static model was found to be equal to (1.9695 MMMSTB).

Pressure and temperature

The Nahr Umr reservoir is an understated reservoir with an initial formation pressure of 4084 psia, which is 2981 psia above its oil bubble point pressure of 1103 psia. The

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reservoir temperature is considered dependent on the eld measurement corrected to the datum level (2500 m SSL) which was found to be equal to 178 F.

Boundary conditions

In this study, ow boundaries from the surrounding aquifer, bottom and edge have been considered as they have proved from well logs, well tests and production log test. The CarterTracy analytical aquifer model (PVT experiments report for Nahr Umr formationSubba oileld 1978) was adopted in the reservoir simulation ow model to represent the water inux drive mechanism. The support expected in this eld was active because the water initially in place volume was found to be more than ten times the oil initially in place.

Fluid properties

The oil had a stock tank gravity of 28 API, and it was highly undersaturated at initial reservoir conditions. The estimated producing gas oil ratio is 389.4 STB/bbl(61.91 m3/m3) based on the laboratory PVT differential liberation experiments and EOS uid modeling results. The oil was of good quality with zero sulfur content. The uid properties of the reservoir are shown in Table 1. For the compositional simulation runs, the PengRobinson cubic equation of state was employed.

Model initialization

The initialization model specied a pressure of 4080 psi at the reference depth of 2500 m. Oilwater relative permeability and capillary pressure data were used. The average reservoir temperature was found to be equal to 178F based on the eld and laboratory measurements at 2500 m.

Capillary pressure and relative permeability

Relative permeability is one of the most important parameters that affect the uid ow in the simulation model. The shape of the Pc and Kr curves, as well as their endpoints, was very important to accurately model uid ow in the reservoir. The water and oil relative permeabilities are two of the most sensitive and important reservoir parameters when evaluating any reservoirs water breakthrough and waterood potential. The relative permeability curves control the relative mobility of the uid phases in the reservoir. They consequently inuence displacement efciency, and, to a lesser extent, sweep efciency. It is critical to obtain reliable and realistic relative permeabilities for input into the simulator. Similar to capillary pressure curves, care should be taken in the preparation of the relative permeability data for the simulation models in order to have a simulation model that runs efciently and accurately. The curves should be smooth and monotonic, and end point saturations between the drainage capillary pressure, imbibition capillary pressure and relative permeability curves should be consistent. In the current study, the measured core laboratory capillary pressure and relative permeability curves were used. However, the capillary pressure was scaled on the basis of the Leverett J-function (Leverett 1941) for the permeability, porosity and interfacial tension.

Airbrine restored state capillary pressure measurements were conducted for ten reservoir core plugs. These experiments data were divided into four groups based on the permeability and connate water saturation of the core plugs. The arithmetic average of the connate water saturation values was assigned to each group. The water saturation values were normalized, and the determination of the corresponding dimensionless Leverett J-function (Ahmed 2005) was used to convert the capillary pressure curves for each group into a universal curve. Four J-function equations were generated for all the rock types. The water saturation values were de-normalized, and the determination of the corresponding Leverett J-functions was generated as a function of the normalized water saturation (Swn)

by selecting arbitrary values of Swn. The resulting Leverett J-functions have been plotted versus the corresponding water saturation. The best-t line for each rock type was nally generated. The resulting capillary pressure (Pc)

equation for each rock type was as follows:

PC 120:12 0:0724 Sw 0:951

Table 1 Reservoir uid properties

T, F 178 Pb, psia 1103

qo, API 28.7

lO @ Pb, cp 1.6183

Bo @ Pb, rbbl/STB 1.189

cx 1.1678 lw, @ Pinit, cp 0.7000

cg 0.6534

Bw @ Pinit, rbbl/STB 1.0160

764:25 0:3

PC 120:12 0:1302 Sw 0:923

245 0:11

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130 0:05

1.0

PC 120:12 0:114 Sw 1:59

0.8

PC 120:12 0:0951 Sw 3:31

30:7 0:015

There were twelve relative datasets of permeability measurements conducted on twelve core samples harvested from 5 wells in the reservoir. The experiments were conducted under ambient conditions using the unsteady state method, with oil and brine as the test uids. Coreys correlations (Corey 1954) were used to make gasoil and wateroil relative permeability curves for the four different rock types in the model and correlate the laboratory data as follows:

krwn Swnwn 6 kron 1 Swnno 7

The weighted average normalization respect to the capacity (kh) was determined for the oil and water relative permeability values as a function of the normalized water saturation by selecting arbitrary values of the normalized water saturation. The corresponding average Corey exponent parameters that matched the average normalized relative permeability curves were then adjusted. The de-normalization process was nally assigned to the different rock types based on the existing connate water saturation (Swc) for each rock type. The values of the residual oil saturations (Sor) and end points relative permeabilities (krw@Sor, and kro@Swc) for each rock type were determined through the weighted average in respect to the (porosity x thickness) and the capacity (kh) for the residual oil saturation and end point relative permeability, respectively. The laboratory measurements of the relative permeability curves suggested that the reservoir rocks were almost behaving as oil wet as supported by the crossover point in the data which mostly occurring at saturations less

than (50 %). Figures 1 and 2 show the capillary pressure and relative permeability curves for the four rock types.

For the gasoil relative permeability, there were 14 sets of relative permeability data measurements conducted on 14 core samples taken from four wells in the reservoir. The same approach followed in the oilwater relative permeability is shown previously was used to create the gasoil relative permeabilities. Figure 3 shows the oilgas relative permeability curves for the two active rock types that were used in the simulation model. In the simulation model, gas and oil were considered as the miscible components that mean that there was no capillary pressure between the oil and gas.

PVT model

The PVT model was accomplished by employing IPMPVTP uid thermodynamic software from Petroleum Experts Ltd. The Podbielniak compositional analyses were conducted for a bottomhole uid sample of the reservoir. The uid properties were calibrated with the EOS compositional model to match the measured laboratory data. Ten components of the reservoir uid sample till C6? were used to generate the cubic PengRobinson EOS as shown in Table 2. The model adjusted the component properties to match the observed uid properties. The elds production separator conditions were incorporated in the PVT model calculations, as indicated in Table 3. Five-stage tests were performed on the uid sample including the stock tank, the liberated GOR and gas specic gravity at each separation step. In the current study, the single stream mode was utilized to match the laboratory data which included the adjusting properties,i.e., the component properties of one stream were changed to match its laboratory data. The component compositions

kro, krw

0.6

0.4

0.2

0.0

0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0

Fig. 2 Relative permeability curves for four rock types in the Nahr Umr reservoir (wateroil system)

4.0

3.5

3.0

2.5

Pc, psi

2.0

1.5

1.0

0.5

0.0

0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0

Saturation, Sw

Rock Type-1 Rock Type-2 Rock Type-3 Rock Type-4 Rock Type-1 Rock Type-2 Rock Type-3 Rock Type-4

Fig. 1 Capillary pressure curves for the Nahr Umr reservoirSubba oileld

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1.0

0.9

kro1 krg1 kro2 krg2

0.8

0.7

kro, krg

0.6

0.5

0.4

0.3

0.2

0.1

0.0

0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0

Fig. 3 Relative permeability curves for two rock types in the Nahr Umr reservoir (gasoil system)

Table 2 Composition of the injected gas

Component Zi (Mole-frac)

N2 0.001 CO2 0.998 C1 0.001

Table 3 Separator stages for the Nahr Umr reservoir

Separator Stage 1 2 3 4 Stock tank

Pressure (psig) 600 255 27 12 0

Temp. (C) 60 60 60 60 60

were kept with no change. The following EOS parameters were adjusted to achieve the match of the global XA and XB (the same value of each was used for all the components), the critical temperature (Tc) and critical pressure (Pc) for the pseudo-components and the nonhydrocarbon components (N2, CO2). The Tc and Pc of the uid components were selected as the regression parameters to be tuned in order to obtain the laboratory data matched for all the uid properties except the uid viscosity, which was predicted separately by using the Lohrenz, Bray and Clark model (Lohrenz et al. 1964). This correlation used the composition, specic gravity and, more importantly, critical volume (Vc), which was the dominated parameter as it was the most signicant input parameter for the model.

It was very unlikely that a satisfactory match to the observed properties would be obtained before applying a multivariable nonlinear regression process. Therefore, a nonlinear regression analysis was carried out to get the match between the laboratory experimental results and the modeled uid properties. The following experimental results were used as match parameters:

1. Bubble point pressure from the differential liberation dataset.

2. Fluid density at the bubble point pressure from the differential liberation dataset.

3. Oil formation volume factor (Bo) versus pressure from the differential liberation dataset.

4. Oil density versus pressure from the differential liberation dataset.

5. Solution of gas oil ratio (Rs) versus pressure from the differential liberation dataset.

6. Stock tank oil density for the differential liberation dataset.

While tuning the EOS, it is important to recognize that the purpose of doing so is to provide a tool which is capable of predicting uid behavior away from the experimental conditions. The combination of the EOS having many parameters to adjust, and the availability of powerful multivariable regression algorithms, means that there is a danger that the EOS can be forced to match the tuning data to such a degree that it cannot predict the behavior under other conditions accurately. In order to avoid this, the regression was limited to those parameters which were known with least certainty and only moderate changes were allowed. In the current study, no components splitting was required to achieve the EOS parameters match because the ten-component PR-EOS description reected a good match to the PVT data. The matched results are presented in Figs. 4, 5, 6, 7 and 8.

Minimum miscibility pressure (MMP)

The minimum miscibility pressure (MMP) is the minimum pressure for a specic temperature at which miscibility can occur independently of the overall composition (El-Maghraby et al. 2011). For the miscible CO2-injection project, the reservoir pressure must be maintained at the minimum miscibility pressure or higher. The MMP is reported to be a function of temperature and uid compositions. Several methods for determination of the MMP have been proposed: slim tube experiments, calculations with EOS and correlations. There was no availability of slim tube experiment results or the experiments required to conduct the EOS analysis for the Nahr Umr reservoir. Therefore, it depended on the available correlations to determine the minimum miscibility pressure. Several empirical correlations were tested, including Glaso (1985), Yellig and Metcalfe (1980), Yuan and Johns (2004), Cronquist (1978) and Alstone (1985); the results are shown in Table 4. The MMP calculated by the Glaso (1985) method was found equal to 2425 psia. This was considered in the current work because, the average molecular weights

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J Petrol Explor Prod Technol (2017) 7:125146 133

Fig. 4 Bubble point pressure match on phase envelope after regression

Fig. 5 Differential liberation oil density match after regression

Fig. 6 Differential liberation gas oil ratio match after regression

Fig. 7 Differential liberation oil formation volume factor match after regression

of the uid samples used the in Glaso correlation, almost near the molecular weight of the Nahr Umr uid and it gave an average value as well.

Economic calculations

To prove the success of any project, economic calculations have to be performed to examine the project feasibility. The technical success of the project alone sometimes is not enough to give the nal decision of the projects success as many projects have proved to be technical successes but not economical ones.

To build a sound business decision, it requires economical criteria for measuring the value of the proposed investments and nancial opportunities (Ganesh and Satter 1994). The objectives of carrying out an economical analysis were to select the best development strategy for the eld based on the minimum costs and high prot. The

net present value is considered as one of the most economical criteria that are widely used to include the time value of money and is considered as a measure of prot. It is dened as the aggregate of all project cash ows for a specied time period, discounted back to a common point in time. In this study, a xed discount rate of 10 % per annum was considered. NPV was determined by calculating the present worth of all the future net cash ows and summing them up. The future cash ow includes all sales revenue of the produced oil and gas minus the costs of water handling, water reinjection, capital expenditures (CAPEX), operational expenditures (OPEX) and transportation cost of oil discounted at a 10 % annual rate. The operation cost escalation was considered to be 1.5 % (Ghomian 2008). This included the lifting cost, water handling, reinjection and recycling costs. The ination rate of the oil prices was considered in this study as it causes prices to rise over time. Oil prices had a big fall in mid-2014 to US$ 44 and stopped falling at the end of the same

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market. Gas prices were assumed to be constant over the project life.

The cost of existing producing wells was considered already incurred during the natural depletion phase of the eld. The royalty and taxes were neglected in this analysis as the oil elds are owned and developed by the Iraqi government. The NPV was computed using the following formula (Ganesh and Satter 1994; Nwaozo 2006):

NPV X

NCFt 1 i

NCF t

Revenue CAPEX OPEX Water handling and reinjection Transpotation cost CO2price CO2Recycle cost

Fig. 8 Differential liberation oil viscosity match after regression

Table 4 Minimum Miscibility Pressure Calculations

Correlation Minimum miscibility pressure (psia)

Glaso (1985) 2425

Yellig and Metcalfe (1980) 2221

Yuan and Johns (2004) 2659

Cronquist (1978) 2894

Alstone (1985) 3269

In a comparison of the NPV prole for different injection modes, it has been hard to present a rigorous decision among them as the NPV prole was changing throughout the production period. Therefore, its another economic criterion was introduced to assist making a sound decision; this economic criterion is called the net present value index (NPVI). The NPVI was very useful to measure the investment and prot efciency, and it was calculated using the following equation:

NPVI

CNPV

MCO 10

In order to perform the NPV and NPVI calculations, the economical parameters shown in Table 5 were used in this study (Al-Khatteeb 2013; Bailey et al. 2000; Al-Mudhafar 2013). The capital expenditures included the cost of production facilities, water injection facilities, injection well drilling, completion, cementing, perforation and acidizing services. The water handling and reinjection processes included: pumping, electricity, treatment equipment, storage equipment, piping and maintenance.

Reliability of the reservoir simulation model

It is essential to conduct miscible ooding for highly a heterogeneous reservoir on a full-eld scale. Webber and Van Geuns (1990) discovered that the geological heterogeneity varies depending on the scale of the measurement. In essence, at a given scale, such as the microscopic level, confuse within the individual reservoir unit, cross-bedding and lamination can be identied and thus have signicant an impact on uid ow. Three wells have been reported to be produced from the reservoir over a short period. The cumulative oil production of these wells was: 1205 STB in

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1-Jan-84 30-Dec-91 28-Dec-99 26-Dec-07 24-Dec-15 22-Dec-23

140

Oil Price

130

120

110

100

USS

Date

Fig. 9 Statistic historic of oil prices

year and then fell again to US$ 36 at the end of 2015 as presented in Fig. 9. The variability of oil prices makes it difcult to expect the exact trend of the ination rate. As oil prices move up or down, ination follows in the same direction. The reason why this happens is that oil is a major input in the economy and it is used in critical activities, such as fueling transportation and heating homes. If the input costs rise, so should the cost of the end products. In this study, a ratio of a 5 % ination rate per annum was assumed to be more reasonable to keep pace with the oil

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Table 5 Economic parameters for the Nahr Umr reservoir

Interest rate (%) 10

Oil price ($/STB) 50

Net gas price ($/MSCF) 3.5

Water handling ($/STB) 0.373

Water re-injection ($/STB) 0.559

OPEX ($/STB) 1.5

Well capex (MM$) 5

Average crude oil transportation cost ($/STB) 2.7

Water injection facilities (MM$) 17

Production facilities (MM$) 100

CO2 capturing and compression ($/MScf) 0.85 CO2 transportation ($/MScf) 0.25 CO2 recycle ($/MScf) 0.35 Capex of CO2 separation, treatment and re-injection (MM$) 22

Fig. 10 History match for well oil productions

3 months, 12269 STB in 6 months and 13816 STB in 6 months. The reliability of the simulation model has been approved through history by matching of these three wells as presented in Fig. 10. The calculated initial oil in place by the simulation model was found to be equal to 2064110111 STB. This value was compared with a corresponding one calculated by the geological model (1969497011 STB). The percentage error was found to be equal to 4.6 %. This conrmed the reliability of the simulation model. It was crucial to gain condence in the numerical models by validating the models and results by use of laboratory results. To obtain a more accurate CO2-compositional simulation model, the capillary pressure and relative permeability needed to be consistent with the permeability/porosity variations of the rocks (Webber and Van Geuns 1990). The published experimental results (El-Maghraby et al. 2011; Krause et al. 2009; Perrin and Benson 2010; Cai and Hicks 1999) revealed the strong dependency of the CO2 saturation distribution on porosity

and permeability heterogeneity. Giraud et al. (1971) and Henry and Metcalfe (1983) reported that the realistic permeability data must be used in evaluating the volu-metric sweep-out. The migration and trapping of injected CO2 are controlled mainly by the interplay of the capillary pressure. Capillary pressure curves and relative permeability curves consistent with the rock properties and heterogeneities should be obtained through a laboratory core analysis (Bennion and Bachu, 2006). In the current study, the permeabilityporosity models were generated based on the core oil/brine experimental results15. The reliability of these models has been approved by comparing the results with the oil/brine experimental results. These models were utilized to generate the permeability for each well interval.

The uid behavior in the miscible compositional simulation model depended mainly on the EOS PVT model which has been approved as discussed in the PVT model section. There were three phases considered in the model, oil, water and gas and the MISCIBLE option, which were activated. The HCSCAL option was activated to allow performing an extra scaling of the hydrocarbon relative permeabilities. Because, in the current study, the gas relative permeability of the connate water differed from the oil relative permeability, a discontinuity occurred in the hydrocarbon relative permeability as the system became two phases. The HCSCAL option scaled krg near the critical point in an analogous manner to the hydrocarbon relative permeability to avoid a discontinuity. In the current study, the considered relative permeability for the oil water and gasoil systems, and capillary pressure analysis were gathered from laboratory measurements. The three-phase relative permeability curves were calculated considering zero residual gas saturation and different residual water and oil saturations for the oilwater relative permeability system. For the gasoil relative permeability system, different residual gas, oil and water saturations were considered.

Composition of the injected uid

In the current study, pure CO2 has injected; however, when simulating CO2-injection with 100 % purity of CO2, problems near-critical conditions will occur, unless the injection uid is diluted to a certain degree. If pure CO2 is injected, no phase envelope will be formed (Tor, 2014);

instead, it will be a straight line. However, if there is a very small fraction of C1 and N2, the mixture will form a phase envelope and Eclipse will have a bigger margin of calculating phase properties. The phase properties should be approximately equal to that of pure CO2 if the fractions of the impurities are very small. The injection gas

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components considered in the current study are shown in Table 2. Moreover, it is important to note that in reality the CO2-injected will always contain some impurities. Additionally, by injecting pure CO2 it may cause the grid blocks to only contain CO2. This causes problems for Eclipse since two or more components are needed to perform a ash calculation.

Waterooding (WF)

The waterooding technique has proved to be the most popular and successful secondary oil recovery mechanism. This recovery method has been used on numerous oil elds worldwide. However, after the secondary recovery process, there is still a signicant amount of oil trapped in the reservoir. In the current study, the waterooding process was tried after the natural depletion of the reservoir. There have been six producers already drilled; these producers were located almost in the middle of the formation. There were 50 inll drillings suggested as the optimum well locations (Al-Khazraji and Shuker 2015a, b). The water-ooding process was achieved through 21 injectors. These injectors were located depending on the reservoir heterogeneity and in a way that would provide enough support to the producers. The waterooding process has been optimized to start in January 2027 as a secondary recovery method after depletion of the reservoir, naturally, for 10 years. Several waterooding options were tried with different injection rates at each injector as follows: 1000, 1250, 1500, 2000, 2500 and 3000 STB/day. The water-ooding process has been optimized to halt in January 2056 and start the miscible CO2-ooding process because of the incomparable oil recovery obtained for different injection rates as shown in Fig. 11. The simulator runs were conducted using the compositional simulator for the compatibility purpose in order to import the restart le data of the waterooding case into the CO2 compositional simulator runs. The setup for the simulation model was the following: All production wells were set on the constant production rate of 3000 STB/day, with a bottomhole pressure limit of MMP for the CO2 injection. The production at the well stopped as the watercut level of 80 % was reached. The injection rates were adjusted to avoid the pressure increase over the formation fracture pressure.

The results are presented in Fig. 11. As it can be seen, the injection rate option of 3000 STB/day has reected the higher reservoir production rate. The results were analyzed economically depending on the NPV calculations; these results are presented in Fig. 12. The higher NPV was also realized at the injection rate option of 3000 STB/day. This case was considered as the base of which the CO2-miscible injection process was continued.

Continuous carbon dioxide injection (CCO2)

This technique involves injecting a certain amount of CO2 continuously until the required slug size is reached. Usually, continuous miscible CO2-injections have excellent microscopic displacement efciency. But, they often suffer from poor macroscopic sweep efciency due to the formation of viscous ngers that propagate through the CO2 passing much of the hydrocarbon that has not been contacted. This happens as a result of the low viscosity of the CO2 compared to the oil, and it results in an adverse mobility ratio.

In this study, the miscible carbon dioxide injection was started up after the waterooding process had been completed. The optimum waterooding strategy was chosen as the base to continue the CO2-injection process. In this issue, several compositional simulation runs were conducted to optimize to the optimum the CO2-injection rate that reected the highest net present value. A wide range of injection rates was trying to examine the reservoir

Fig. 11 Reservoir performance under different waterood scenarios

-50

NPV_1000 STB/Day

NPV_1250 STB/Day

NPV_1500 STB/Day

NPV_2000 STB/Day

NPV_2500 STB/Day

NPV_3000 STB/Day

injection

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NPV, $MM

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Date

Fig. 12 NPV for different waterood scenarios

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Fig. 13 Reservoir performance comparison under different CO2-

ooding scenarios

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NPVI

200

NPV-5 NPV-10 NPV-15 NPV-20 NPV-25 NPV-30 NPV-35 NPV-40 NPV-45 NPV-50 NPV-2.5 NPV-1 NPV-1.25 NPVI-5 NPVI-10 NPVI-15 NPVI-20 NPVI-25 NPVI-30 NPVI-35 NPVI-40 NPVI-45 NPVI-50 NPVI-2.5 NPVI-1.25 NPVI-1

550

175

150

450

125

NPV, $MM

350

100

250

150

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Date

Fig. 14 NPV and NPVI for different continuous CO2 scenarios

Table 6 Water injection rate for different WAG ratio

NO CO2-WAG Qwinj STB/day

1 1:1 9643

2 1.5:1 14465

3 1:1.5 6432

4 1:2 4822

5 1:2.5 3857

6 1:3 3211

7 1:3.5 2758

8 1:4 2411

performance under the miscible CO2-injection. These rates included: 5, 10, 15, 25, 40 and 50 MM Scf/day. The setup for the simulations was the following: All production wells were set at the constant production rate of 3000 STB/day, with the bottomhole pressure limit of MMP. The CO2 was injected at a constant rate for each development strategy, with the maximum bottomhole injection pressure limit of the formation fracture pressure. The production wells were closed when the watercut reached the limit of 95 %, and the injection rates were adjusted to avoid a pressure increase over the fracture pressure. All the results were analyzed relative to the net present value calculations as the economic criterion.

The results showed that the injection rate option of 50 MScf/day has reected the higher oil recovery for the rst 6 years of the reservoir production as shown in Fig. 13. But economically, the injection rate option of 20 MScf/day has reected the higher NPVI as shown in Fig. 14. This

injection rate was considered as an optimal CO2-injection rate for all the CO2-ooding modes.

Water-alternating-CO2-injection (CO2-WAG)

The CO2-WAG technique is a combination of two traditionally improved oil recovery techniques: waterooding and gas injection. The waterooding and gas ooding cycle lengths are alternated with the design parameters being the cycle timing of the WAG process and the ratio of water to gas, slug size of the injected CO2 and water. The main advantage of this technique is to reduce the CO2 channeling by lling the highly permeable channels with water to improve the macroscopic sweep efciency during the CO2-injection. The optimum conditions of the oil displacement by the WAG processes are achieved when the velocities of the gas and water are the same in the reservoir and hence stabilize the sweeping front. The optimum WAG design varies from reservoir to reservoir depending on the reservoir heterogeneity and characteristic. The main advantages of the WAG process include reduced CO2 utilization and production, and greater ultimate recovery.

In the current study, the CO2-WAG injection process proceeded after the waterooding process has completed.

Under this strategy, several compositional simulation runs were modeled to optimize the CO2-WAG process for the

Nahr Umr reservoir. The setup for the simulations was the following: All production wells were set at the constant production rate of 3000 STB/day, with the bottomhole pressure limit of MMP. The production wells were closed when the watercut reached the limit of 95 %, and the injection rates were adjusted to avoid a pressure increase over the fracture pressure.

Two cases were considered here; the rst one included utilizing the economically optimum CO2-injection rate determined in the CCO2-injection process of 20 MM Scf/day. Eight cases with different CO2-WAG ratios were

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Fig. 15 Reservoir performance comparison under different CO2-

WAG ratio ooding scenarios

200

NPV-1:1.5 NPV-1:1 NPV-1:4 NPV-1.5:1 NPV-1:2.5 NPV-1:3.5 NPV-1:3 NPV-1:2 NPVI-1:1.5 NPVI-1:1 NPVI-1:4 NPVI-1.5:1 NPVI-1:2.5 NPVI-1:2 NPVI-1:3 NPVI-1:3.5

$600

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NPVI

175

$520

150

$440

2ratio

Bw 11

Hybrid-CO2-WAG injection

This technique is achieved when a large slug of CO2 was injected followed by a number of small slugs of water and

CO2. In the current study, this technique has been achieved by utilizing the optimum CO2-WAG injection mode portion and the optimum injection rate for the initial CO2-injection rate. The effects of varying the initial CO2 slug size on the recovery factor for the hybrid CO2-WAG were studied. The setup for the simulations was the following:

All production wells were set at a constant production rate of 3000 STB/day, with the minimum bottomhole pressure of MMP. The production wells were closed when the watercut reached the limit of 95 %, and the injection rates for the water and CO2 were adjusted to avoid a pressure increase over the formation fracture pressure.

Five trials with varying initial CO2 slugs, including 10, 20, 30, 40, and 50 % HCPV, were modeled. The initial

CO2 slug size was dened by prolonging the cycle time of the initial CO2-injection until the required initial CO2 slug size was met. The required slug size in terms of HCPV is presented in Table 7. The results are presented in Figs. 19 and 20. It was shown that the mode of the initial CO2 slug size of 10 % injection reected the higher NPVI and oil production.

125

$360

NPV, $MM

$280

100

$200

$120

$40

-$40

Date

Fig. 16 NPV and NPVI for different CO2-WAG ratio scenarios

Fig. 17 Reservoir performance comparison under different CO2-

WAG cycle length scenarios

simulated and evaluated. They were 1:1, 1:1.5, 1:2, 1:2.5, 1:3, 1:3.5, 1:4, 1.5:1 and 2:1. The corresponding water injection rate for each CO2-WAG ratio was determined by utilizing Eq. (11) as the CO2-injection rate remained constant as shown in Table 6. The cycle lengths for each phase of all eight trials were set for a year. The results showed that the CO2-WAG process option of a 1.5:1 CO2-WAG ratio has reected the higher oil recovery and NPVI at the same time as shown in Figs. 15 and 16.

The second case included utilizing the optimum CO2-WAG ratio to investigate the optimum CO2-WAG injection for varying the cycle time. Eight trials were considered, including 3, 6, 9, 12, 18, 24, 30 and 36 months half-cycle lengths for each phase. All the results were analyzed relative to the net present value calculations. The results showed that the CO2-WAG injection with a 1.5:1 CO2-

WAG ratio and 12 months half-cycle lengths has reected

the higher oil recovery and NPVI at the same time as shown in Figs. 17 and 18.

QCO2 BCO2 WACO

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$640

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NPVI

200

NPV-6month

NPV-9month

NPV-12month

NPV-18month

NPV-24month

NPV-30month

NPV-36month

NPV-3month

NPVI-6month

NPVI-9month

NPVI-12month

NPVI-18month

NPVI-24month

NPVI-30month

NPVI-36month

NPVI-3month

$600

$560

175

$520

$480

150

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$400

NPV, $MM

125

$360

$320

$280

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$240

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-$40

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Fig. 18 NPV and NPVI for different CO2-WAG cycle length scenarios

Table 7 Hydrocarbon pore volume required for hybrid WAG process

No CO2 slug Size % HCPV rbbl Period day

1 10 187855561.6 913

2 20 375711123.2 1826

3 30 563566684.8 2739

4 40 751422246.4 3652

5 50 939277808.0 4565

6 60 1127133370 5479

7 70 1314988931 6392

8 80 1502844493 7305

9 90 1690700054 8218

10 100 1878555616 9131

Fig. 19 Reservoir performance comparison under different Hybrid CO2-WAG injection scenarios

200

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NPVI

175

$520

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$440

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NPV, $MM

$360

$280

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$120

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-$40

Date

NPV-10 % HCPV NPV-20 % HCPV NPV-30 % HCPV NPV-40 % HCPV NPV-50 % HCPV NPVI-10 % HCPV NPVI-20 % HCPV NPVI-30 % HCPV NPVI-40 % HCPV

Fig. 20 NPV and NPVI for different Hybrid CO2-WAG scenarios

Simultaneous water and CO2-injection (CO2-SWAG)

This technique involves injecting water and CO2 in combination into the reservoir at the same well. The mixing of

CO2 and water in a CO2-SWAG injection can be at the downhole or on the surface. Surface mixing usually occurs at the well, drill site or at the central processing facility. The objective of this technique is to improve the sweep efciency of the CO2-ooding by reducing the impact of viscous ngering. At the same time, this reduces the capital and operating costs and nally will result in an improvement in gas handling and oil recovery (Ma et al. 1995; Sanchez 1999). The simultaneous water and gas injection can be difcult to implement and there can be some practical difculties associated with this technology.

In this study, the CO2-SWAG process was tested through ve modeled compositional simulation runs to analyze the effects of different CO2-injection rates for the

CO2-SWAG injection on the recovery factor. The setup

for the simulations was the following: All production wells were set at a constant production rate of 3000 STB/day, with the minimum bottomhole pressure of MMP. The production wells were closed when the watercut reached the limit of 95 %, and the injection rates for the water and CO2 were adjusted to avoid a pressure increase over the formation fracture pressure. To determine the optimum CO2-SWAG injection rate, the CO2-

SWAG ratio was xed at 1:1 and the accompanying water injection rates were determined using Eq. (11). The CO2-injection rates considered for this case were: 5000, 7500, 10000, 12500 and 15000 MScf/day. The accompanying water injection rates were calculated using Eq. (11) as shown in Table 8.

The results have been presented in Figs. 21 and 22. It can be seen that the CO2-SWAG process option of 15000

MScf/day CO2-injection and 7232 STB/day water injection has reected the higher oil recovery and NPVI at the same time.

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Table 8 Water injection rate for different SWAG process

NO WACO2 QCO2 MScf/day Qwinj STB/day

1 1:1 5000 9643

2 1:1 7500 14465

3 1:1 10000 6432

4 1:1 12500 4822

5 1:1 15000 3857

Fig. 21 Reservoir performance comparison under different CO2-

SWAG scenarios

225

Table 9 Water injection rate for different SWAG ratio

NO WACO2 QCO2 MScf/day Qwinj STB/day

1 1:1 15000 7232

2 1:2 15000 3616

3 1:3 15000 2408

4 1.5:1 15000 10849

5 2:1 15000 14465

650

1-Jan-55

NPV, $MM

NPV-2411+5

NPV-3616+7.5

NPV-4822+10

NPV-6027+12.5

NPV-7232+15

NPVI-2411+5

NPVI-3616+7.5

NPVI-4822+10

NPVI-6027+12.5

NPVI-7232+15

550

450

350

250

150

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Date

Fig. 22 NPV and NPVI for different CO2-SWAG scenarios

In order to determine the optimum CO2-SWAG ratio on the recovery factor, ve CO2-SWAG ratios were simulated and evaluated. They were 1:1, 1:2, 1:3, 1.5:1 and 2:1. The optimum CO2-SWACO2 injection rate calculated from the previous step (15000 MScf/day) was used as a constant. But, the accompanying water injection rate was varied for all of the ve cases according to their water to the CO2-

SWACO2 ratio. The required water injection rates to make up the CO2-SWAG ratio were calculated using Eq. (11) as shown in Table 9.

The results are presented in Figs. 23 and 24. It can be seen that the CO2-SWAG process option of a 2:1 CO2-

SWAG ratio has reected the higher NPVI and oil recovery at the same time.

Results and discussion

Heterogeneous reservoirs are known to have a low recovery factor due to pressure development within the reservoir, multiphase phase behavior, reservoir compartmentalization, capillary pressure and viscosity effect (Bennion and Bachu, 2006). The results reected a successful CO2-ooding process in all modes because the obtained recovery factors were in the expected range. However, many wells were closed during the prediction period due to reaching the watercuts the maximum limit and causing a reduction in the oil recovery. For CCO2-ooding modes, it was observed that by increasing the CO2-injection rate, an increase in the eld oil production rate (FOPR) at an earlier stage was achieved. However, the ultimate FOPR stayed in approximately the narrow range after 8 years of the predicted period. This was due to the development of a gas channel between the injectors and producers. From Figs. 25, 26 and 27, it can be seen that by implementing the CCO2-ooding with the lower injection rate set to 5

MMScf/day, the injected amount of CO2 was not enough to achieve efcient displacement. The injection rate of 20 MMScf/day reected a consistent, efcient oil sweeping as the distribution of the injected CO2 was almost uniform in the reservoir. Therefore, the stabilized displacement gave an upward shift in the NPV and NPVI curves, Fig. 14. In the case of a high CO2-injection rate with a 50 MMScf/day, the CO2-injected distribution exhibited higher CO2 saturation in the reservoir, especially in the parts of high connectivity (indicated by the red color). This led to developing gas channels in the reservoir, especially in the part of high connectivity. In this case, the channeling of gas was more prominent and a lot of gas was back produced. This explained getting a high produced GOR during the predicted period. As more CO2 was produced as the unstable displacement front and more separation and recycling cost was required, hence, there was a reduction in the project protability.

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Fig. 23 Reservoir performance comparison under different CO2-

SWAG ratio scenarios

250

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NPVI

225

550

200

450

175

NPV, $MM

150

350

125

250

100

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DateNPV-1:3 NPV-1:2 NPV-1.5:1

NPV-2:1 NPV-1:1 NPVI-1:3 NPVI-1:2 NPVI-1.5:1 NPVI-2:1 NPVI-1:1

Fig. 24 NPV and NPVI for different CO2-SWAG ratio scenarios

Fig. 25 CO2-distibution for CO2-injection rate set to 5000 MScf/day at Jan/2072

Fig. 26 CO2-distibution for CO2-injection rate set to 20000 MScf/day at Jan/2072

For the WAG injection scheme, the CO2-WAG ooding with a low WAG ratio of 1:4 reected the less oil recovery and protability. This reected that lower mobility control of CO2 had been occurring and then bypassed a large amount of oil. As the WAG ratio increased to a certain extent, the oil recovery and economic feasibility improved. This reected the improvement in gas mobility control through increasing the amount of injected water. Moreover, the low WAG ratio caused early gas breakthrough and gas channeling; hence, oil was trapped and not allowed sufcient gasoil contact. The WAG ratio of 1.5:1 reected the highest oil recovery and economic feasibility. From Figs. 28, 29 and 30, it can be seen that the CO2 saturation distribution for the second case was higher and consistent which means that there were stable microscopic displacement and mobility control for CO2. At the same time, the macroscopic displacement was better managed in this case. This amount of water was sufcient to realize the mobility control and stable displacement front. The one-year half

cyclic length reected the highest oil recovery and economic feasibility, although the CO2 saturation distribution did not exhibit an appreciable difference for different cyclic lengths. The economic analysis shows an outperformance of a 1-year half cycle over the others. However, the 1-year half cyclic length is considered more convenient, practically, to apply than the shorter cycles. This process was tried till a 31.6 % HCPV CO2 slug size had been injected for the date January 2072. If the process continues longer, the expected oil recovery increment will be higher. The simulation time was limited to January 2072 due to the length of time it would take and large computational cost if the predicted time was extended. It is worth noticing that it was difcult to differentiate between different CO2-WAG injection processes based on oil recovery alone without combining the results with the economic analysis. Figures 31, 32 and 33 show the CO2 saturation distribution for this case.

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142 J Petrol Explor Prod Technol (2017) 7:125146

Fig. 27 CO2-distibution for CO2-injection rate set to 50000 MScf/day at Jan/2072

Fig. 28 CO2-distibution for WAG ratio set to 14 at Jan/2072

Fig. 29 CO2-distibution for WAG ratio set to 12 at Jan/2072

Fig. 30 CO2-distibution for WAG ratio set to 1.51 at Jan/2072

In the CO2-SWAG process, it has been concluded that the gas efciency factor (incremental oil produced per volume of gas injected) decreases with larger gas injection volumes. The optimum amount of the injected gas has to be used. From Figs. 34, 35, 36 and 37, it can be seen that the saturation of CO2 was less compared to the other CO2-injections modes, as the required amount of injected CO2 was also less. Accordingly, the reduced injected slug size led to reduced project cost, hence increased protability for the SWAG process. In conclusion, the injection water, in alternating slugs or simultaneously with gas forms, yields a more stable displacement front, hence better project profitability over other CO2-injection modes. The water phase acts for more mobility control of gas, hence better microscopic displacement.

In the case of the hybrid CO2-WAG injection, the one of a 10 % initial CO2 slug size injection reected a higher

NPV and oil production among the other hybrid WAG modes. With the greater CO2 slug size injection, the more

inconsistent the sweep efciency was, due to the unfavorable mobility of the CO2 and the reservoir heterogeneity.

The incremental oil recovery for the hybrid process was less than that for the CCO2 process; but, the economic protability of the hybrid process was better due to the large cost of the required injected CO2 in the case of the

CCO2 process. As compared to the WAG process, the incremental oil recovery for the hybrid process was0.189 % less. The gas injection alone often resulted in poor sweep efciency due to the early breakthrough caused by the unfavorable gasoil mobility ratio. This explained the outperformance of the hybrid process of the 10 % HCPV injection slug over the others as the large solvent slug sizes, per WAG cycle, caused channeling and increased cost, substantially. The minimizing of the slug size, per WAG cycle, maximized the protability of the solvent oods. The solvent contacted more oil, and channeling was minimized when the CO2 slug size, per WAG cycle, was decreased. However, the achieved oil recovery by the

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J Petrol Explor Prod Technol (2017) 7:125146 143

Fig. 31 CO2-distibution for WAG cyclic length set to 6 month at Jan/2072

Fig. 32 CO2-distibution for WAG cyclic length set to 12-month at Jan/2072

Fig. 33 CO2-distibution for WAG cyclic length set to 24-month at Jan/2072

Fig. 34 CO2-distibution for CO2-SWAG rate set to 2411 bbl/day (water) and 5 MMScf/day (CO2) at Jan/2072

Fig. 35 CO2-distibution for CO2-SWAG rate set to 6072 bbl/day (water) and 12.5 MMScf/day (CO2) at Jan/2072

Fig. 36 CO2-distibution for SWAG ratio set to 13 at Jan/2072

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Fig. 37 CO2-distibution for SWAG ratio set to 21 at Jan/2072

250

$650

1-Jan-55 31-Dec-58 30-Dec-62 29-Dec-66 28-Dec-70

NPVI

$550

200

NPV, $MM

$450

150

$350

$250

100

$150

$50

-$50

Date

NPV-WAG 1.5-1 NPV-CO2-20 MMScf/day NPV-CO2-10 %-Hybrid NPV-SWACO2-2:1 NPV-WF-3000 STB/day NPVI-WAG 1.5-1 NPVI-CO2-20 MMScf/day NPVI-CO2-10 %-Hybrid NPVI-SWACO2-2:1 NPVI-WF-3000 STB/day

Fig. 38 NPV for different CO2-ooding modes and waterooding scenarios

WAG and SWAG processes was higher than the corresponding one of the CCO2-ooding processes. This conrmed the improvement in the sweep efciency by stabilizing the displacement front, and in particular, it was helpful in severe heterogeneity, gravity overrides and reduction in the capillary entrapment of the oil.

In this study, it was observed that the vast majority of producers became wet very soon and the water production

increased for most of them. This required the use of an articial lift method to keep the wells production and enhance oil recovery. However, the objective here has been to investigate the contribution of the CO2-injection modes individually to improve oil recovery. In conclusion, the CO2-SWAG mode of the 2:1 SWAG ratio has reected the higher NPVI over other CO2-injection modes. The incremental oil recovery from the CO2-SWAG process was9.174 % higher than the waterooding case, 1.113 % in comparison with the CCO2-ooding case, 1.176 % in comparison with the hybrid CO2-WAG case and almost0.987 % when compared with the CO2-WAG case. The results have been shown in Fig. 38 and Table 10.

Observations and conclusions

The observations and conclusions drawn from this study are summed up below:

1. This study is enough to give answers to what will be the performance of Nahr Umr reservoir and other clastic heterogeneous reservoirs in the southern of Iraq under miscible CO2-ooding processes.

2. The MMP calculated by the Glaso (1985) method was considered in the current work because the average molecular weights of the uid samples utilized in preparing the Glaso correlation were almost near the molecular weight of the Nahr Umr reservoir uid. Moreover, it gave an average value among the other correlations.

3. The CCO2 has resulted in the poorest economic protability in front of the other CO2-injection modes, whereas WAG and SAWG processes have resulted in better performance.

4. As the reservoir heterogeneity increases, there is a need to apply WAG and SWAG process implementation to increase oil recovery.

5. It is necessary to conduct a detailed economic analysis to prove the most effective process among different CO2-injection modes.

6. The CO2-injections modes have fullled expectations.

Table 10 NPVI for different development options

Injection mode

Producers Injectors Period years

FOE (%) NPVI

WF 56 21 28 0 3000 51.89 451.19642 22.524 59.0057

CCO2 56 21 16 20 0 83.39 569.8769 30.585 158.4938 CO2-WAG 56 21 16 20 3000 83.08 582.5244 30.711 197.3218 Hybrid-CO2-WAG 56 21 16 20 3000 83.93 575.3267 30.522 166.0301 SWG-Diff-CO2-rate 56 21 16 20 3000 83.61 590.9341 30.703 201.4182 SWG-Diff-SWAG ratio 56 21 16 20 3000 86.70 611.5333 31.698 229.4477

Gas Inje. rate (MMScf/Day)

Water Inje. rate (STB/Day)

WC (%) Cum. oil

MMSTB

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J Petrol Explor Prod Technol (2017) 7:125146 145

7. The SWAG injection process proved as a means to provide better mobility control of gas than the WAG injection.

8. The oil production rate for all CO2-ooding scenarios showed the typical behavior with the increase in the oil production at the beginning of injection period and then a drop because the production wells were closed, due to reaching the watercut limit. Therefore, it requires application the articial lift means to enhance oil recovery.

Acknowledgments Our thanks mainly go to the Iraqi Ministry of Oil for permission to publish this paper and to the PETRONAS Oil Company that has supported this work.

Open Access This article is distributed under the terms of the Creative Commons Attribution 4.0 International License (http://creativecommons.org/licenses/by/4.0/

Web End =http:// http://creativecommons.org/licenses/by/4.0/

Web End =creativecommons.org/licenses/by/4.0/ ), which permits unrestricted use, distribution, and reproduction in any medium, provided you give appropriate credit to the original author(s) and the source, provide a link to the Creative Commons license, and indicate if changes were made.

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Carbon dioxide flooding is considered one of the most commonly used miscible gas injections to improve oil recovery, and its applicability has grown significantly due to its availability, greenhouse effect and easy achievement of miscibility relative to other gases. Therefore, miscible CO2-injection is considered one of the most feasible methods worldwide. For long-term strategies in Iraq and the Middle East, most oilfields will need to improve oil recovery as oil reserves are falling. This paper presents a study of the effect of various CO2-injection modes on miscible flood performance of the highly heterogeneous clastic reservoir. An integrated field-scale reservoir simulation model of miscible flooding is accomplished for this purpose. The compositional simulator, Eclipse compositional, has been used to investigate the feasibility of applying different miscible CO2-injection modes. The process of the CO2-injection was optimized to start in January 2056 as an improved oil recovery method after natural depletion and waterflooding processes have been performed, and it will continue to January 2072. The minimum miscibility pressure was determined using empirical correlations as a function of reservoir crude oil composition and its properties. Four miscible CO2-injection modes were undertaken to investigate the reservoir performance. These modes were, namely the continuous CO2-injection (CCO2), water-alternating-CO2-injection (CO2-WAG), hybrid CO2-WAG injection, and simultaneous water and CO2-injection (CO2-SWAG) processes. All injection modes were analyzed in respect to the net present value (NPV) and net present value index (NPVI) calculations to confirm the more feasible CO2 development strategy. The results indicated that the application of CO2-SWAG injection mode of 2:1 SWAG ratio attained the highest oil recovery, NPV and NPVI, among the other modes. The achieved incremental oil recovery by this process was 9.174 %, that is 189 MM STB of the oil produced higher than the waterflooding case, 1.113 % (23 MMSTB of oil) in comparison with the CCO2-flooding case, 1.176 % (24.3 MMSTB of oil) in comparison with the hybrid CO2-WAG case and almost 0.987 % (204 MMSTB of oil) when compared with the CO2-WAG case. The results indicated that the application of CO2-WAG injection mode of 1.5:1 WAG ratio attained the highest oil recovery after the SWAG process.

Details

Title

Field-scale investigation of different miscible CO2-injection modes to improve oil recovery in a clastic highly heterogeneous reservoir

Author

Jaber, Ahmed Khalil; Awang, Mariyamni B

Pages

125-146

Publication year

2017

Publication date

Mar 2017

Publisher

Springer Nature B.V.

ISSN

21900558

e-ISSN

21900566

Source type

Scholarly Journal

Language of publication

English

DOI

https://doi.org/10.1007/s13202-016-0255-5

ProQuest document ID

1869046586

Journal of Petroleum Exploration and Production Technology is a copyright of Springer, 2017.

Field-scale investigation of different miscible CO2-injection modes to improve oil recovery in a clastic highly heterogeneous reservoir

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