Experimental Measurements and Numerical Simulation of H₂S Generation during Cyclic Steam Stimulation Process of Offshore Heavy Oil from Bohai Bay, China

Abstract

Cyclic steam stimulation (CSS) is successfully applied to increase heavy oil recovery in heavy oil reservoirs in Bohai Bay, China. However, during the CSS processes, hydrogen sulfide (H₂S) was detected in some heavy oil reservoirs. The existing literature mainly focused on the H₂S generation of onshore heavy oil. There is no concrete experimental data available, especially about the level of H₂S generation during CSS of offshore heavy oil. In addition, there is still a lack of effective reaction kinetic models and numerical simulation methods to simulate H₂S generation during the CSS of offshore heavy oil. Therefore, this paper presents a case study from Bohai Bay, China. First, the laboratory aquathermolysis tests were conducted to simulate the gases that are produced during the CSS processes of heavy oil. The effects of the reaction temperature and time on the H₂S generation were studied. Then, a one-dimensional CSS experiment was performed to predict H₂S generation under reservoir conditions. A kinetic model for the prediction of H₂S generation during the CSS of heavy oil was presented. The developed model was calibrated with the experimental data of the one-dimensional CSS experiment at a temperature of 300 °C. Finally, a reservoir model was developed to predict H₂S generation and investigate the effects of soaking time, steam quality, and steam injection volume on H₂S generation during CSS processes. The results show that the H₂S concentration increased from 0.77 ppm in the first cycle to 1.94 ppm in the eighth cycle during the one-dimensional CSS experiment. The average absolute error between the measured and simulated H₂S production was 12.46%, indicating that the developed model can accurately predict H₂S production. The H₂S production increase with soaking time, steam quality, and steam injection volume due to the strengthened aquathermolysis reaction. Based on the reservoir simulation, the H₂S production was predicted in the range of 228 m³ to 2895 m³ within the parameters of this study.

1. Introduction

Recently, due to the gradual depletion of onshore oil resources and the growing global energy demand, the exploitation of offshore heavy oil resources has attracted much attention [1,2,3]. Bohai Bay, China, has abundant heavy oil resources with approximately 4 billion tons [4,5]. Cyclic steam stimulation (CSS) is successfully applied to increase heavy oil recovery in heavy oil reservoirs in Bohai Bay, China [6,7]. However, during the CSS processes, hydrogen sulfide (H₂S) was detected in some heavy oil reservoirs [8]. H₂S generation can even reach up to 0.044%. H₂S generation from production operations is a concern in CSS recovery of offshore heavy oil because H₂S poses a hazard to health, affects the integrity of wellbore tubulars, and impacts surface facility design considerations [9,10,11]. Therefore, it is necessary to predict H₂S production prior to CSS implementation.

The generation of H₂S has attracted considerable attention because of its toxicity and corrosiveness. Hyne and Greidanus defined the chemical reaction between oil sand and steam as an aquathermolysis reaction and considered that the C–S bond cleavage of S-containing organic compounds in oil sands was an important step in the aquathermolysis reaction [12]. Clark et al. used tetrahydrothiophene as a model compound for aquathermolysis reactions, revealing the reaction path of tetrahydrothiophene cracking to H₂S [13]. Perez-Perez et al. proposed a kinetic model to predict the H₂S generation and deduced the evolution of H₂S in resins and asphalt of heavy oil [14]. Kapadia et al. developed an aquathermolysis kinetic model for Athabasca bitumen to predict H₂S concentrations, and the kinetic model was also validated against a wide range of laboratory and field data (Assabaska Oilfield, Canada) [15]. Furthermore, Zhao et al. conducted aquathermolysis experiments with minerals and concluded that the H₂S concentration was higher when minerals were present in the aquathermolysis reaction mixture. Besides, they also reported that the reaction temperature of aquathermolysis could be reduced due to this catalytic effect [16]. Na et al. carried out aquathermolysis experiments with bitumen samples in a H₂S corrosion-resistant autoclave and found that the amounts of H₂S generated increased with an increase in the reaction time and temperature [17]. Meanwhile, Ma et al. conducted aquathermolysis experiments of LH residual oil and reported that the use of superheated steam is effective in promoting H₂S generation [18].

The aforementioned literature mainly focused on the H₂S generation of onshore heavy oil. There is no concrete experimental data available, especially about the level of H₂S generation during the CSS of offshore heavy oil. In addition, almost all of the aforementioned aquathermolysis tests were performed under static conditions by the reactors. The fluid displacement and the effects of reservoir rocks were not taken into account. There is still a lack of effective reaction kinetic models and numerical simulation methods to simulate H₂S generation during the CSS of offshore heavy oil. In addition, numerous experiments were conducted and found that the heavy oil quality (chemical group composition, viscosity, and gas composition) was improved after aquathermolysis processes [19,20]. However, the H₂S generation during the experimental process was not investigated. Therefore, this paper presents a case study from Bohai Bay, China. First, the laboratory aquathermolysis tests were conducted to simulate the gases that are produced during CSS recovery of heavy oil. The effects of the reaction temperature and time on the H₂S generation were studied. Then, a one-dimensional CSS experiment was conducted to predict H₂S generation. A kinetic model for the prediction of H₂S generation during the CSS of heavy oil was presented. The developed model was calibrated with the experimental data of the one-dimensional CSS experiment at a temperature of 300 °C. Finally, a reservoir model was developed to predict H₂S generation and investigate the effects of soaking time, steam quality, and steam injection volume on H₂S production during CSS.

2. Experiment

2.1. Experimental Materials

The heavy oil was collected from an offshore heavy oil reservoir. The basic properties and composition of the heavy oil are shown in

Table 1. Basic properties and composition of heavy oil.

Viscosity at 323 K (mPa⋅s)	Density at 323 K (kg/m3)	Molecular Weight (g/mol)	Composition
			S, %	H, %	N, %	C, %	Others, %
1232	955.977	600	0.368	11.07	0.723	80.649	7.19

. The water used in this study was distilled water. Silica sand with a particle size of 200 μm was used as porous media to prepare the sandpack model in the CSS experiment. N₂ with a purity of 99.99% was provided by Qingdao Xinkeyuan Technology Co., Ltd., Qingdao, China.

2.2. Experimental Setup

2.2.1. Aquathermolysis Experiments

The setup of the aquathermolysis experiments is detailed in Figure 1. The aquathermolysis experiments were performed in a closed autoclave reactor (Anhui Kemi Machinery Technology Co., Ltd., Hefei, China). The 300 mL reactor was made of Hastelloy C276, and its maximum operating pressure and temperature can achieve 34.5 MPa and 500 °C, respectively. A thermal control system was used to control the temperature of the autoclave reactor by an electric furnace and displayed the temperature data transmitted by an internal temperature probe in real time. A pressure gauge (Jasco 25-1009-SW-02L-400BR-X6W) with a range of 0–40 MPa was used to monitor the pressure during each experiment. The top of the reactor was equipped with a magnetic stirrer with stirring fluid, and a circulating water bath was provided to prevent the magnetic stirrer from being damaged at high temperatures. A vacuum pump was applied to empty the air in the system in advance to improve the accuracy of the experiments. Before each experiment, a certain amount of heavy oil and water were weighed by an electronic balance, and nitrogen was used as an eluent gas. After each experiment, 500 mL gas bags were used to collect the gas products. A gas chromatograph (7890A, Agilent CO., Ltd., Santa Clara, CA, USA) equipped with a flame ionization detector (FID) and sulfur chemiluminescence detector (SCD) was used to analyze the composition of gas products.

2.2.2. One-Dimensional CSS Experiment

The setup of the one-dimensional CSS experiment is shown in Figure 2. The CSS experiment was performed in a one-dimensional sandpack model (3.8 cm in diameter and 48 cm in length) made of Hastelloy C276. Its maximum operating pressure and temperature were 50 MPa and 450 °C, respectively. The pump was used to inject water and heavy oil into the sandpack model. Its minimum injection rate can reach 0.01 mL/min. The steam generator was used to heat the water provided by a pump to the specified injection temperature, and its maximum working pressure and the temperature reached 35 MPa and 450 °C, respectively. A temperature control system was used to control the sandpack model temperature by six belt heaters (power 3500 W) surrounded by the sandpack surface, and a pressure probe together with a computer was used to monitor the sandpack pressure. The products were cooled to 60 °C through the cooling system and condenser to avoid damage to the back-pressure regulator (BPR). The BPR, together with a hand pump, was used to adjust the sandpack model pressure. The gas–liquid separator separated the products into the liquid and gas phases. An electronic balance and a gas meter were used to measure the mass of the liquid and gas volume. The gas was collected in 500 mL gas bags and analyzed by the gas chromatograph.

2.3. Experimental Procedures

2.3.1. Aquathermolysis Experiments

The autoclave reactor with 50 g heavy oil and 25 g water was sealed. Inspection for leakage was completed after N₂ was used to evacuate the air in the autoclave reactor (repeated three times). Then, the thermal control system controlled the electric furnace to heat the reactor at a rate of 8 K/min. When the temperature reached 100 °C, the magnetic stirrer started to stir the fluid in the reactor at a stirring rate of 600 rpm. After the temperature in the reactor reached the predetermined experimental temperature, the reactor was heated at a constant temperature for a certain reaction time. Once the aquathermolysis reaction was completed, the reactor was rapidly cooled with forced air to avoid the influence of steam on the experimental results. Finally, the gas products were collected in 500 mL gas bags and analyzed by the gas chromatograph. According to the aforementioned process, a series of aquathermolysis experiments were conducted to examine the effects of temperature (270 °C and 300 °C) and time (0.5 d and 2 d) on gas products.

2.3.2. One-Dimensional CSS Experiment

The silica sand was filled in the clean one-dimensional sandpack model. After the experimental setups were connected, inspection for leakage and vacuuming were completed. The temperature control system controlled the band heater to heat the sandpack model to 46 °C (reservoir temperature). Then, the pump was used to inject water and heavy oil into the sandpack model, and the porosity, permeability, and initial oil saturation of the model were measured, which were 56.8%, 2748 mD, and 85.4%, respectively. After the sandpack model preparation was finished, the steam generator heated the distilled water to the predetermined temperature (300 °C), and the steam near 100% quality was injected into the model at a rate of 10 mL/min until the reservoir pressure reached the desired pressure. After steam injection, the model was soaked till pressure was stable. The time of steam injection and soaking in each cycle was 2 h in total. During production, the BPR was used to control the outlet pressure, and 1 MPa/h was applied as a pressure drop rate in each cycle. The whole cycle finished when the model pressure was 1 MPa. The CSS cycles were repeated until the end of the eighth cycle. The mass of liquid and gas volume was measured by the electronic balance and the gas meter, and the gas products at the end of cycle 1, cycle 4, and cycle 8 were collected in 500 mL bags, respectively. Finally, the collected gas products were analyzed by the gas chromatograph.

2.4. Experimental Results and Discussion

2.4.1. Aquathermolysis Experiments

Table 2. Results of gas chromatography for gas products at different reaction temperatures and times.

Gas Composition	270 °C, 0.5 d	300 °C, 0.5 d	270 °C, 2 d	300 °C 2 d
	Volume, %	Volume, %	Volume, %	Volume, %
H2	38.52	39.437	39.519	40.265
CO2	24.487	26.935	27.192	30.861
CO	0.499	0.812	1.253	1.476
Methane	12.921	15.446	16.507	18.792
Ethane	2.381	3.419	2.861	3.906
Ethylene	3.22	2.795	2.184	0.237
Propane	2.516	2.824	3.11	3.618
Propylene	2.456	1.235	1.195	0.302
Isobutane	0.185	0.147	0.153	0.114
N-butane	0.73	0.577	0.458	0.159
Trans-2-butene	3.658	2.186	2.679	0.051
1-butene	1.964	1.225	0.763	0.012
Isobutene	0.928	0.254	0.278	0.035
Pentane	0.327	0.135	0.186	0.022
Isopentane	0.154	0.086	0.095	0.037
Pentene	1.256	0.14	0.507	0.008
C6+	3.797	2.343	1.056	0.093
H2S	0.00013	0.003185	0.003029	0.01019

shows the results of gas chromatography for the gas products. It can be seen from Table 2 that the concentrations of H₂S, CO₂, and H₂ were 0.00013% (1.3 ppm), 24.487%, and 38.52%, respectively, at 270 °C and 0.5 d.

The possible reasons for the presence of H₂S, CO₂, and H₂ in the gas products are shown as follows [12]:

$$\mathrm{Organosulfur}\stackrel{\mathrm{Aquathermolysis}}{\to }{\mathrm{Alcohol}+\mathrm{Mercaptan}+\mathrm{H}}_2\mathrm{S}$$

(1)

$$\mathrm{Alcohol}\stackrel{\mathrm{Aquathermolysis}}{\to }\mathrm{Aldehydes}$$

(2)

$$\mathrm{Aldehydes}\stackrel{\mathrm{Aquathermolysis}}{\to }\mathrm{Carbon}\mathrm{Monoxide}+\mathrm{Hydrocarbon}$$

(3)

$$\mathrm{Carbon}\mathrm{monoxide}+\mathrm{Steam}\stackrel{\mathrm{WGSR}}{\to }\mathrm{Carbon}\mathrm{dioxide}+\mathrm{Hydrogen}$$

(4)

$$\mathrm{Hydrogen}+\mathrm{Organosulfur}+\mathrm{Mercaptan}\stackrel{\mathrm{Hydrodesulfurization}}{\to }{\mathrm{H}}_2\mathrm{S}$$

(5)

According to Equations (1)–(5), it can be seen that the C–S bond of the S-containing organic compound of heavy oil broke in the aquathermolysis reaction, resulting in the presence of H₂S, CO₂, and H₂ in the gas products.

Of course, many paraffin hydrocarbons and olefins were also detected in the gas products. For example, the concentrations of methane, ethane, and propane were 12.921%, 2.381%, and 2.516%, respectively, while the concentrations of C₆₊, pentene, and trans-2-butene were 3.797%, 1.256%, and 3.658%, respectively at 270 °C and 0.5 d. Similar results were observed in the other three sets of experiments. The possible reasons are shown as follows: (1) The C–C bond cleavage of asphalt chains and the β scission in the alkyl side chain of aromatics of heavy oil lead to the formation of short olefins and low molecular light hydrocarbon in the aquathermolysis reaction [21,22]. (2) The extraction of steam resulted in the formation of long-chain hydrocarbons (such as C₆₊, trans-2-butene, pentene, and so on) in the gas products [23].

Besides, it can be seen from Table 2 that the H₂S concentration increases with the increase in temperature. When the reaction time was 0.5 days, the H₂S concentrations were 0.00013% (1.3 ppm) and 0.003185% (31.85 ppm) at 270 °C and 300 °C, respectively. This is due to the fact that with the increase in temperature, the reaction rate accelerated, and the C–S bond was easier to break. In addition, the concentrations of CO₂ and H₂ also varied from 24.487% and 38.52% to 26.935% and 39.437%, respectively. Similar results were observed when the reaction time was 2 d. The significant increase in the concentrations of CO₂ and H₂ also proves that an increasing temperature is beneficial for the aquathermolysis of heavy oil. Due to the accelerated aquathermolysis reactions, light hydrocarbons (methane, ethane, and propane) increased, and heavy hydrocarbons (pentene, trans-2-butene, and C₆₊) decreased with the increase in temperature.

Table 2 also shows the results of the aquathermolysis reaction at different reaction times. The H₂S concentration increased with the increase in reaction time. When the reaction time varied from 0.5 d to 2 d at 300 °C, the H₂S concentration increased from 0.003185% (31.85 ppm) to 0.01019% (101.9 ppm). The concentrations of CO₂ and H₂ also increased from 26.935% and 39.437% to 30.861% and 40.265%, respectively. The results suggest that increasing time deepened the degree of aquathermolysis.

According to the experimental data of the aquathermolysis experiments, the activation energy and frequency factor were estimated by a Kapadia kinetics model [15]. As shown in Figure 3a, the reaction time had a linear relation with the concentrations of H₂S [24]. The reaction time and the concentration of H₂S were fitted, with the slope of the regression lines showing the values of reaction rates (k) at different temperatures. It can be seen from Figure 3a that the reaction rates at 300 °C and 270 °C are 0.0000467 and 0.00001933, respectively. Figure 3b shows the relationship between the reaction rates (k) and temperatures (T). The corresponding kinetic parameters (activation energy and frequency factor) were obtained according to the slope and intercept of the interpolation line (Figure 3b), which are 76.12 kJ/mol and 404.03 1/day, respectively.

2.4.2. One-Dimensional CSS Experiment

The results of the one-dimensional CSS experiment are shown in Figure 4. As shown in Figure 4a, the sandpack model pressure increased during the steam injection. Once the target pressure was reached, the soaking began, and then the sandpack model pressure tended to be stable. When the soaking was completed, the pressure decreased at 1 MPa/h. In addition, as the CSS cycle increased, the oil production gradually dropped while the water cut gradually increased (Figure 4b). The oil recovery at the end of the eighth cycle reached 40.10% (Figure 4a).

The results of gas chromatography are shown in

Table 3. Results of gas chromatography during the CSS process.

The First Cycle		The Fourth Cycle		The Eighth Cycle
Composition	Volume, %	Composition	Volume, %	Composition	Volume, %
CO2	98.080	H2	0.316	H2	0.475
Methane	1.274	CO2	93.698	CO2	89.769
Ethane	0.095	Methane	2.176	Methane	3.043
Ethylene	0.137	Ethane	0.422	Ethane	0.536
Propane	0.162	Ethylene	0.575	Ethylene	0.670
C6+	0.248	Propane	0.413	Propane	0.508
H2S	0.000077	Propylene	0.406	Propylene	0.457
		Isobutane	0.158	Isobutane	0.135
		Trans-2-Butene	0.137	Trans-2-Butene	0.194
		Pentane	0.384	N-butane	0.568
		Pentene	0.256	1-butene	0.159
		C6+	1.054	Isopentane	0.402
		H2S	0.00019	Pentane	0.961
				Pentene	0.720
				C6+	1.400
				H2S	0.000194

. It can be seen from Table 3 that the H₂S concentration increased from 0.000077% (0.77 ppm) in the first cycle to 0.000194% (1.94 ppm) in the eighth cycle during the one-dimensional CSS experiment. This is because the injected amount of steam increased as the oil was produced, resulting in stronger aquathermolysis reactions. However, it is noted that, after the fourth cycle, the amount of oil saturation was gradually reduced. Therefore, the concentration of H₂S at the end of the eighth cycle was only 0.000004% higher than that at the end of the fourth cycle. In addition, the relative volume of CO₂ decreased from 98.08% to 89.769% due to the generation of more types of gases during the aquathermolysis reactions and steam extraction.

3. Numerical Simulation

3.1. One-Dimensional Numerical Simulation

3.1.1. Building the One-Dimensional Numerical Simulation Model

In this study, CMG-STARS software was used to develop a numerical model to simulate the H₂S generation during the one-dimensional CSS experiment. According to the size of the one-dimensional sandpack model, a one-dimensional numerical simulation model was established, as shown in Figure 5. Reasonable grid size and step size can not only approach reality, but also improve the operational speed of the grid model. Therefore, the one-dimensional numerical simulation model included 48 × 19 × 19 (17328) grids, and the grid size was 1 cm (X) × 0.2 cm (Y) × 0.2 cm (Z). The reservoir properties (porosity, permeability, oil saturation) were obtained from the experimental data, and

Table 4. The reservoir fluid and rock properties used in the model.

Parameters	Values
Reservoir temperature, °C	46
Reservoir pressure, kPa	8000
Rock compressibility, 1/MPa	4 × 10−5
Rock heat capacity, J/(m3·°C)	2.58 × 106
Thermal conductivity of rock, J/(m3·d·°C)	1.634 × 105
Thermal conductivity of water phase, J/(m3·d·°C)	5.99 × 104
Thermal conductivity of oil phase, J/(m3·d·°C)	9.77 × 103
Thermal conductivity of gas phase, J/(m3·d·°C)	1.9 × 103

shows the other reservoir and rock properties used in the model.

In this study, the fluid model was set up with three components: water, heavy oil, and H₂S. The density and oil volume factors of heavy oil are 955.977 (kg/m³) and 1.035, respectively. The viscosity–temperature curve of heavy oil, oil–water relative permeability curve, and gas–liquid relative permeability curve adopted in the model are shown in Figure 6 and Figure 7.

The kinetic parameters (activation energy and frequency factor) used in the numerical simulation model were obtained from the aforementioned studies (Figure 3), and the following reaction Equation (6) was applicable to describe the generation of H₂S during the CSS process.

Heavy Oil→H₂S

(6)

The production parameters of wells in the model are consistent with the operating parameters during the one-dimensional CSS experiment.

3.1.2. History Matching

Taking the cumulative oil production and H₂S production of the one-dimensional CSS experiment as the fitting targets, the matching was carried out by mainly adjusting the relative permeability curve and kinetic parameters, such as activation energy and frequency factor in the developed numerical simulation model. As shown in Figure 8, the simulated cumulative oil production and H₂S production are consistent with those obtained by experiments. The average absolute errors between the measured and simulated cumulative oil production and H₂S production were 4.31% and 12.46%, respectively. All the results indicate that the measured and simulated H₂S production had a good consistency, and the developed model can accurately predict H₂S production during CSS processes. Therefore, the calibrated parameters were used to predict H₂S production in the following reservoir numerical simulation.

3.2. Reservoir Numerical Simulation

Prediction of H₂S Production

There is a heavy oil reservoir in Bohai Bay, China, at depths of 800 to. 1000 m, with porosities of 12–45%, average permeabilities of 2450 mD, and initial oil saturation of 70–82%. In the reservoir model, to consider the reasonable running time, the total number of cells in the three-dimensional (3D) model was equal to 20,000. The oil layer was vertically subdivided into 10 zones. The reference depth of the reservoir simulation model was set equal to 800 m with pressure at 8000 kPa. Basic reservoir properties and operational parameters for the 3D reservoir model are shown in

Table 5. Reservoir properties and operational parameters used in the simulation model.

Parameter	Values
Porosity	0.12–0.45
Average permeability, mD	2450
Initial oil saturation, %	70–82
Oil volume factor	1.035
Cyclic steam injection volume, m3	7500
Steam temperature, °C	300
Steam quality	0.7
Steam injection rate, m3·d−1	250
Soaking time, d	5
Cycles	5

. The relative permeability curves and kinetic parameters obtained from the history matching of the one-dimensional CSS experiment are directly applied to the reservoir simulation.

Based on the established reservoir model, the H₂S production during the CSS process of offshore reservoirs was predicted, ranging from 228 m³ to 1490 m³ (Figure 9). However, it is noted that the H₂S production decreases with the increase of cycles after two cycles. This is attributed to the fact that the continuous production of heavy oil near-wellbore leads to a decrease in the amount of S-containing organic compounds, resulting in a weakened aquathermolysis reaction.

3.3. Sensitivity Analysis

3.3.1. Effects of Steam Quality

Figure 10 shows the effects of steam quality on H₂S production. It can be found from Figure 10 that the production of H₂S has an increasing trend with the increase in steam quality. The maximum H₂S production is 2895 m³ when the steam quality is 1. This is because the steam with higher quality has a high latent heat of vaporization and a large specific volume. When the steam was injected into the reservoir, the steam with a higher steam quality accelerated the aquathermolysis reaction and increased the H₂S production.

3.3.2. Effects of Soaking Time

Figure 11 shows the effects of soaking times (1–5 days) on H₂S production. As shown in Figure 11, the production of H₂S increases gradually with the increase in soaking time. The reason for this trend is that with the increase in soaking time, the time of aquathermolysis reaction increases. Therefore, the extent of the aquathermolysis reaction is gradually deepened. However, the increasing degree of H₂S production gradually decreases with the increase in soaking time after the third cycle. The reason is that the oil saturation near-wellbore decreases after the continuous aquathermolysis reactions.

3.3.3. Effects of Steam Injection Volume

Figure 12 shows the effects of steam volumes on H₂S production. It can be seen from Figure 12 that the production of H₂S increases from 652 m³ to 1490 m³ as steam injection volume increases from 5500 m³ to 7500 m³ per cycle. It is because the aquathermolysis reaction of heavy oil is more intense due to the existence of more steam and higher heat.

4. Conclusions

(1)

The concentrations of H₂S increased with the increase in temperature and time. The aquathermolysis reaction resulted in the presence of H₂S, CO₂, and H₂ in the gas products. The effects of the oil–water ratio, rock minerals, and pressure on the concentrations of H₂S need to be further investigated, and the oil products after the aquathermolysis need to be comprehensively analyzed in future research.

(2)

The established kinetic model can be used to predict H₂S production during the CSS processes. The activation energy and frequency factor were estimated to be 76.12 KJ/mol and 404.03 1/day, respectively.

(3)

The H₂S concentrations increased from 0.77 ppm to 1.94 ppm during the one-dimensional CSS experiment. As the CSS cycle increased, the oil production gradually dropped while the water cut gradually increased. The oil recovery at the end of the eighth cycle reached 40.10%.

(4)

The measured and simulated H₂S production had a good consistency, indicating that the developed model has high precision in predicting H₂S production during CSS processes.

(5)

The H₂S production increased with the increase in soaking time, steam quality, and steam injection volume due to the strengthened aquathermolysis reactions. Based on the reservoir simulations, the H₂S production was predicted in the range of 228 m³ to 2895 m³ within the parameters of this study.