Gas sweetening is one of the important purification processes which is employed to remove acidic contaminants from natural gases prior to meet transport requirements and sale gas specifications. In this work, simulation and parametric studies of the natural gas processing plant of Missan Oil Company/Buzurgan Oil Field of Natural Gas Processing Plant (in Iraq) were considered. After simulation and validation of this plant, the effect of feed temperature and flow rate and solvent concentration were considered. Results show with increasing the feed temperature and flow rate, the amount of H2S and CO2 in the sweet gas stream increases. Then, in the next step, the effect of mixture solvents was studied. Sulfolane–MDEA and MDEA–MEA were selected as a physical–chemical mixture solvent and chemical mixture solvent, respectively. The simulation results show that the solvent price and reboiler duty and cooling duty can be reduced by using a mixture solvent. However, the amount of H2S and CO2 in the sweet gas can be affected by these solvents. The system by a chemical mixture solvent can better performance than other solvents.
-The removal of acid gases, CO 2 and H 2 S from natural gas streams is essential for environmental and health reasons. In this work, the simulated gas sweetening unit with MethylDiEthanolAmine (MDEA) solvent was studied to improve quality. Firstly, the effect of trays types and then, the effect of various packing and the effect of the packing size were considered on the flow rate of CO 2 and H 2 S in the main streams. Results show that with considering the different trays types in the regenerator tower, the flow rate of CO 2 in the sweet gas stream with bubble cap tray is lower than other trays types. Also, with considering the different trays types in the absorber tower, the flow rate of CO 2 in the sweet gas stream with bubble cap tray is lower than other trays types in the absorber tower. In considering with different types of packing, results show that the flow rate of CO 2 with ballast ring packing and the flow rate of H 2 S with Raschig ring packing are lower than other types of packing. However, in some types such as cascade miniring, Intalox Saddles and pall ring, there is no difference for the flow rate of CO 2 or H 2 S. In all cases, with increasing the size of the packing, the flow rate of CO 2 and H 2 S in the sweet gas stream increases, however, this increasing in the metal packing is very small.
The three-dimensional oil-water flow in horizontal pipe has been investigated by introducing population balance equation (PBE). The water fraction of inlet flow and mixture velocity varies from 46% to 60% and from1.25 m/s to 3m/s, respectively. The multiple size groups model has been applied to the non-uniform drop size distribution in oil-water flow. The drop coalescence models have a clear efficacy on the prediction capability of the PBE. In this work, drop coalescence model for oil-water is modified and used for predicting the phase distribution of dispersed oil-water in horizontal pipe. Population balance with modified Coulaloglou's frequency model is used. The attention of the modification is on the presence of droplets that reduce the free space for droplet motion and cause an enhancement in the collision frequency. The phase distribution profile from numerical results is presented and discussed. Acceptable agreement with the experimental data is achieved by using the modified coalescence model. Also, at 46% water fraction and mixture velocity equal as 3 m/s, model with population balance with modified Coulaloglou is 4% and 1% better than Luo's model and Coulaloglou's model, respectively.
Flow distribution and pressure drop in parallel micro-channels are two effective parameters on the performance of different devices. These two parameters are affected by different factors, such as the manifold geometry, channels geometry, flow rate and fluid direction of inlet flow. In the present work, the structure of the inlet manifold (the triangular geometry, with straight and curved walls) has been studied as the main subject. However, the effect of the flow rate (as the Reynolds number) and fluid direction of inlet flow has been studied on the flow distribution and pressure drop with these manifold geometries. The results show that in the low-Reynolds number range, with increasing the Reynolds number, the flow distribution does not change, but the pressure drop increases. Also, the vertical direction of the inlet flow in comparison with the horizontal direction is preferable. Flow distribution with triangular manifolds with curved walls is more uniform than with straight walls, while, in straight walls, equilateral triangle is a better choice. At the end of this consideration, the effect of geometry parameters (such as the channel number, channel width and depth of curvature) on the non-uniformity parameter was studied with concave manifolds.
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