A method for measuring the rheology of crude oil in equilibrium with carbon dioxide at reservoir conditions is presented.
A rheometer system to measure the rheology of crude oil in equilibrium with carbon dioxide (CO2) at high temperatures and pressures is described. The system comprises a high-pressure rheometer which is connected to a circulation loop. The rheometer has a rotational flow-through measurement cell with two alternative geometries: coaxial cylinder and double gap. The circulation loop contains a mixer, to bring the crude oil sample into equilibrium with CO2, and a gear pump that transports the mixture from the mixer to the rheometer and recycles it back to the mixer. The CO2 and crude oil are brought to equilibrium by stirring and circulation and the rheology of the saturated mixture is measured by the rheometer. The system is used to measure the rheological properties of Zuata crude oil (and its toluene dilution) in equilibrium with CO2 at elevated pressures up to 220 bar and a temperature of 50 °C. The results show that CO2 addition changes the oil rheology significantly, initially reducing the viscosity as the CO2 pressure is increased and then increasing the viscosity above a threshold pressure. The non-Newtonian response of the crude is also seen to change with the addition of CO2.
In most of the literature on the physical properties of CO2 and crude oil mixtures, viscosity is measured using a viscometer, meaning that the measurement is made at a constant shear rate or shear stress. In these studies, the viscosity of CO2 and crude oil mixture is investigated in a simple way: the focus of interest is the relations between the viscosity and other parameters, such as temperature, pressure and CO2 concentration. The key assumption made in these studies, yet rarely mentioned explicitly, is that the CO2 and crude oil mixture behaves as a Newtonian fluid. However, it is well known that some crude oils, especially heavy crude, can show non-Newtonian behavior under certain conditions1,2,3,4. Therefore, to fully understand the CO2 effect, the viscosity of CO2 and crude oil mixture should be studied as a function of shear rate or stress.
To our knowledge, only the study by Behzadfar et al. reports the viscosity of a heavy crude oil with CO2 addition at different shear rates using a rheometer5. In the measurement by Behzadfar et al., the mixing between CO2 and crude oil is achieved by the rotation of the inner cylinder of the coaxial cylinder geometry, a very slow process. In addition, the effect of the CO2 dissolution on the rheology of polymer melts has been reported in the literature, which could shed light on the study of heavy crude oil and CO2 mixtures. Royer et al. measure the viscosity of three commercial polymer melts at various pressures, temperatures and CO2 concentrations, using a high-pressure extrusion slit die rheometer6. They then analyze the data through the free volume theory. Other similar studies can be found in Gerhardt et al.7 and Lee et al.8. Our method, where mixing is performed in an external mixer and the rheology measurement in a coaxial cylinder geometry, allows a more thorough measurement of the rheology of CO2 and crude oil mixture.
The circulation system that we developed contains four units: a syringe pump, mixer, gear pump and rheometer, as shown in Figure 1 and Figure 2. A stirring bar is placed at the bottom of the mixer and magnetically coupled with a rotating magnet set. Stirring is used to enhance the mixing between CO2 and crude oil in the mixer, speeding up the approach to equilibrium between the phases. The CO2 saturated oil phase is withdrawn from close to the bottom of the mixer using a dip tube and circulated through the measurement system.
The viscosity is measured by a high-pressure cell mounted on a rheometer. There are two types of pressure cells. One is with a coaxial cylinder geometry, which is designed for the measurement of viscous fluid; and the other is with a double gap geometry for low viscosity application.
Figure 1: The scheme of the circulation system with coaxial cylinder geometry pressure cell. The blue line represents CO2 flow, and the black line represents the crude oil mixtures. Reprinted with permission from Hu et al.14. Copyright 2016 American Chemical Society. Please click here to view a larger version of this figure.
Figure 2: The scheme of the circulation system with double gap geometry pressure cell. The blue line represents CO2 flow, and the black line represents the crude oil mixtures. Please click here to view a larger version of this figure.
Figure 3: The coaxial cylinder geometry pressure cell. Please click here to view a larger version of this figure.
The coaxial cylinder geometry pressure cell (Figure 3) has a 0.5 mm gap between the inner and outer cylinder, leading to a sample volume of 18 mL. The inner cylinder is magnetically coupled with a rotational cup, which is attached to the rheometer spindle. There are two sapphire bearings at the top and bottom of the inner cylinder, which are directly in contact with the rotation axis of the inner cylinder. Since the sapphire bearings are exposed to the sample by design, the bearing friction may vary according to the lubrication properties of the sample.
Figure 4: The double gap geometry pressure cell. Please click here to view a larger version of this figure.
On the other hand, the double gap pressure cell comprises a cylindrical rotor in a double gap geometry, as illustrated by Figure 4. The measuring cylinder is mounted on the pressure head through two ball bearings and magnetically coupled with the rotation cup, which is connected to the rheometer spindle. The ball bearings are located inside the pressure head and not in contact with the sample, which is injected into the measurement gap and overflows into a recess in the stator from which it is returned to the mixing vessel.
In a typical experiment, the crude oil sample is first loaded into the mixer. After priming the entire system with the crude oil, the remaining volume in the system is evacuated using a vacuum pump. The CO2 is then introduced into the mixer through the syringe pump and the system brought to the desired temperature and pressure. The system pressure is controlled through the CO2 phase by the syringe pump. When the pressure stabilized, the stirrer is turned on to mix the CO2 and crude oil inside the mixer. Then the gear pump is turned on to withdraw the oil phase from the mixer, fill the rheometer and recycle the fluid back to the mixer. Therefore, the mixing between CO2 and crude oil is done by simultaneously stirring in the mixer and circulating in the loop. The equilibrium status is monitored by periodic measurement of both the volume in the syringe pump and the mixture viscosity. When there is no change (≤4%) in both the volume and viscosity, the equilibrium is confirmed. At that stage the gear pump and stirrer are turned off, suspending the flow through the measurement cell and the rheology measurement is carried out.
Note: Since the experiment operates at high temperature and pressure, safety is paramount. The system is protected against over-pressure by the software limit on the syringe pump controller and bursting discs at the mixer and between the gear pump and the rheometer (see Figure 1 and Figure 2). Furthermore, before each experiment, it is recommended to perform a regular leak check. It is also recommended to perform the friction check of the pressure cell geometry to make sure the rheometer is functioning well9,10.
1. Preparing the Crude Oil Sample
NOTE: Use the Zuata crude oil sample as received. The following table shows the basic physical properties of the Zuata crude oil.
Characteristics | Value |
API Gravity | 9.28 |
Barrel Factor (bbl/t) | 6.27 |
Total Sulphur (% wt) | 3.35 |
Reid Vapor Pressure (kPa) | 1 |
Pour Point (°C) | 24 |
Existing H2S Content (ppm) | – |
Potential H2S Content (ppm) | 115 |
Potential HCl Content (ppm) | – |
Calc. Gross Cal. Value (kJ/kg) | 41,855 |
Table 1: The physical properties of the Zuata crude oil.
2. Loading the Crude Oil Sample into the Mixer
3. Priming the Entire System with the Crude Oil Sample
4. Evacuating the Remaining Volume in the System
5. Introducing CO2 into the Mixer
6. Setting the Temperature and Pressure
7. Turning on the Stirrer and Gear Pump
8. Monitoring the Volume in the Mixer and the Mixture Viscosity
9. Performing the Rheology Measurement
10. Increasing the Pressure to the Next Desired Value
The rheology measurement of the Zuata crude oil and its CO2 saturated mixture, at 50 °C using the coaxial cylinder geometry pressure cell, is shown by Figure 5 and Figure 6. Figure 5 shows the measurement from ambient to 100 bar, while Figure 6 shows the measurement from 120 bar to 220 bar. Furthermore, Figure 7 illustrates the relative viscosity, which is the ratio of the viscosity at a given shear rate to the viscosity at the lowest shear rate. The dashed lines in Figure 7 are the maximum measurement error caused by the friction of the bearings of the geometry.
The rheology measurement at 50 °C of the diluted Zuata crude oil, using double gap geometry pressure cell, is illustrated by Figure 8 and Figure 9, while Figure 10 shows the relative viscosity for pressure up to 70 bar. Furthermore, Figure 10 shows that the diluted crude oil at ambient pressure behaves as a Newtonian fluid. However, when the CO2 pressure is from 30 bar to 60 bar, the shear thinning effect is observed. At CO2 pressure above 60 bar, the shear thinning disappears and the mixture behaves as a Newtonian fluid again.
Den Figure 5 and Figure 6 one can see that the CO2 dissolution significantly decreases the viscosity of the crude oil mixture until 100 bar. When the CO2 pressure is beyond 100 bar, the oil mixture viscosity increases with increasing CO2 pressure, but at a much lower rate.
Figure 7 reveals that the Zuata crude oil shows a shear thinning effect without CO2 addition. When CO2 is dissolved into the crude oil, the shear thinning effect is weakened, given that the curves at higher CO2 pressures are flatter. At CO2 pressures higher than 40 bar, the viscosity change with shear rate is within the measurement error range, thus the mixture can be considered to be Newtonian. CO2 dissolution weakens and eventually eliminates the shear thinning effect of the Zuata crude oil. This indicates that the CO2 molecule dissolved into the crude oil can eventually disrupt the associating network generated by the macromolecules in the crude oil, such as asphaltenes.
Regarding the diluted crude oil as shown by Figure 8, the CO2 addition dramatically reduces the oil mixture viscosity to a minimum at 70 bar. As the CO2 pressure increases beyond 70 bar (Figure 9), the higher CO2 pressure causes an increase in the oil viscosity.
According to the study by Seifried et al.11, in both the original and diluted Zuata crude oil, the onset of asphaltene precipitation occurs at CO2 pressures above 80 bar. However, in our rheology experiments when the pressure is higher than 80 bar, the crude oil/CO2 mixture behaves as a Newtonian fluid. This implies that asphaltene precipitation does not alter the rheological properties of this mixture.
The rheology results for the diluted crude oil are also interesting: in this case CO2 dissolution gives rise to the non-Newtonian behavior, which only appears in a certain range of CO2 pressure. Two speculations are given here for the shear thinning effect induced by CO2 addition.
The first speculation is that the non-Newtonian behavior is caused by micelles formed by the asphaltene molecules under CO2 dissolution. The CO2 dissolved in the crude oil can reduce the critical micelle concentration (CMC) of the system by its action on the structure of asphaltene aggregates, and this can lead to greater interaction between micelles12. At pressures from 30 to 60 bar, the distance between asphaltene micelles may be within the effective range of the van der Waals attraction force13. Thus, an associating network is formed among the micelles and causes the shear thinning effect. However, when the pressure is above 60 bar, CO2 effect on the solvent or the non-asphaltene molecules is dominating, which leads to increase the CMC. Therefore, the asphaltene micelles are destabilized, and consequentially the associating network disappears.
The second speculation is based on the phase behavior point of view. At CO2 pressures between 30 and 60 bar, a CO2 rich liquid phase may have been generated, which makes the mixture form a liquid-liquid-vapor (LLV) system. An emulsion of these two liquids could be formed through the mixing by stirring and circulation due to the similar density of the two liquid phases. As the dispersed phase of the emulsion, the CO2 rich liquid phase may be stabilized by the asphaltene in the crude oil. This emulsion shows non-Newtonian behavior because the dispersed phase gives rise to an associating network. However, when more CO2 is dissolved into the oil mixture at pressure above 60 bar, the two liquid phases become miscible again. The result is a liquid-vapor (LV) system comprised of a crude oil rich liquid in equilibrium with a CO2 rich vapor and the crude oil rich liquid phase behaves as a Newtonian fluid.
Figure 5. Viscosity measurement for the Zuata heavy crude oil with CO2 at 50 °C and various shear rates. , lower shear rate limit; , ambient; , 20 bar; , 40 bar; , 60 bar; , 80 bar; , 100 bar. Reprinted with permission from Hu et al.15. Copyright 2016 American Chemical Society. Please click here to view a larger version of this figure.
Figure 6. Viscosity measurement for the Zuata heavy crude oil with CO2 at 50 °C and various shear rates. , lower shear rate limit; , 120 bar; , 140 bar; , 160 bar; , 180 bar; , 200 bar; , 220 bar. Reprinted with permission from Hu et al.15. Copyright 2016 American Chemical Society. Please click here to view a larger version of this figure.
Figure 7. The relative viscosity for the Zuata crude oil with CO2 at 50 °C and various shear rates. – –, measurement fluctuation range; , ambient pressure; , 20 bar; , 40 bar; , 60 bar; , 80 bar; , 100 bar; , 120 bar; , 140 bar; , 160 bar; , 180 bar; , 220 bar. Reprinted with permission from Hu et al.15. Copyright 2016 American Chemical Society. Please click here to view a larger version of this figure.
Figure 8. Viscosity measurement for the diluted crude oil with CO2 at 50 °C and various shear rates. , lower shear rate limit; , 1 bar; , 10 bar; , 20 bar; , 30 bar; , 40 bar; , 50 bar; , 60 bar; , 70 bar. Please click here to view a larger version of this figure.
Figure 9. Viscosity measurement for the diluted crude oil with CO2 at 50 °C and various shear rates. , lower shear rate limit; , 80 bar; , 100 bar; , 120 bar; , 140 bar; , 160 bar; , 180 bar; , 200 bar; , 220 bar. Please click here to view a larger version of this figure.
Figure 10. The relative viscosity for the diluted crude oil with CO2 at 50 °C and various shear rates. – –, measurement fluctuation range; , 1 bar; , 10 bar; , 20 bar; , 30 bar; , 40 bar; , 50 bar; , 60 bar; , 70 bar. Please click here to view a larger version of this figure.
Two steps are critical in the operation. The first one is priming the entire system by the crude oil sample. By filling up the system with the crude oil sample, the gear pump can be well lubricated by the oil sample, and any blockages in the circulation loop can be easily identified. Thus the gear pump can be prevented from damage. The second critical step is periodically monitoring the mixture viscosity to confirm the equilibrium between the CO2 and crude oil. Given that it takes a considerable amount of time to reach the equilibrium between CO2 and viscous heavy crude oil16, performing the rheology measurement too early will underestimate the effect of CO2 addition on the oil viscosity. Therefore, only when the viscosity measured reaches a constant value (less than 4% change), can the mixture be considered in equilibrium with CO2.
The current measurement system only allows the rheology measurement of the CO2 saturated mixture. To measure under-saturated mixtures, an upstream vessel could be introduced to the CO2 stream. The CO2 will be introduced to the upstream vessel first and then isolated from the source, so that the amount of CO2 can be controlled by the volume and pressure in the upstream vessel. The total pressure of the system in this case would be controlled by an inert gas, such as helium. Kariznovi et al. provides a good review on the apparatus used to measure the physical properties of CO2 and heavy crude oil mixture17. Modifications can refer to the systems that reviewed in their paper.
It should be mentioned that the system described here can measure the rheology of any gas-liquid mixtures; therefore its application is not limited to crude oils. For example, it can be used to measure the CO2 effect on the rheology of Pickering emulsions18,19 and gas-induced plasticization6. By introducing the electrical conductivity measurement device into the rheometer pressure cell, the effect of gas dissolution on the shear-induced phase inversion of emulsions could also be studied20,21,22,23.
The authors have nothing to disclose.
The authors gratefully acknowledge funding from the Qatar Carbonates and Carbon Storage Research Centre (QCCSRC), provided jointly by Qatar Petroleum, Shell, and Qatar Science and Technology Park. The authors thank Frans van den Berg (Shell Global Solutions, Amsterdam, Netherlands) for providing the crude oil sample.
Heavy Crude Oil | Shell | N/A | Produced from the Zuata oil flied. Used without further treatment |
Toluene | Sigma-Aldrich | 244511-2L | Anhydrous, 99.8%. Used without further treatment |
CO2 | BOC | 111304-F | CP Grade. Used without further treatment |
Name | Company | Catalog Number | Yorumlar |
Syringe Pump | Teledyne ISCO | 65D | |
Mixer | Parr Instruments | 4651 | Vessel volume 250 ml. Mounted on a series 4923EE bench-top heater |
Gear Pump 1 | Polymer Systems Inc. | CIP-12/1.5 | Used with CC29/Pr pressure cell for high viscosity fluids. |
Gear Pump 2 | Micropump | GAH X21 | Used with DG35.12/Pr pressure cell for low viscosity fluids. |
Rheometer | Anton Paar | MCR301 | |
Pressure cell 1 | Anton Paar | CC29/Pr | With flow-through configuration. Used for high viscosity fluids. Coaxial cylinder geometry |
Pressure cell 2 | Anton Paar | DG35.12/Pr | With flow-through configuration. Used for low viscosity fluids. Double gap geometry |