Simulation of Sour Water Stripping Unit in Oil Refinery with Consideration of Ammonia Separation
In this research, the sour water unit and its simulation were investigated. Sour water unit of refineries usually has two stripping towers in series. The results of this study showed that with the increase in the volumetric flow rate of the incoming sour water feed, the molar flow of NH3 in the exit...
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Semnan University
2024-12-01
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| Series: | مجله مدل سازی در مهندسی |
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| Online Access: | https://modelling.semnan.ac.ir/article_9174_9bf3c51e3ab2ac727fecf1ff53dabfd9.pdf |
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| author | Hassan Shahidi Mehrab Fallahi |
| author_facet | Hassan Shahidi Mehrab Fallahi |
| author_sort | Hassan Shahidi |
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| description | In this research, the sour water unit and its simulation were investigated. Sour water unit of refineries usually has two stripping towers in series. The results of this study showed that with the increase in the volumetric flow rate of the incoming sour water feed, the molar flow of NH3 in the exit gases from the first tower increases. With increasing feed temperature, the NH3 and H2S do not change much until the temperature of 1050C, and after that, the relative molarity of these two substances in the exhaust gases decreases with increasing temperature. By increasing the reflux to the first tower to about 9 m3/hr, the molar flow rate of NH3 gas in the first tower decreases drastically, which actually increases the purity of H2S in the exit gases of this tower and increases the flow of this component in the exit gases from the second tower. Also, with the increase in the temperature of the end of the tower, the flow of NH3 and H2S increases and at a temperature of about 120 0C, all the H2S in the feed enters the exit gases from the first tower and the exit water from the first tower is free of H2S. As a result, it can be concluded that the best temperature for the bottom of the first tower is about 120 0C so that all the H2S is removed from the water and NH3 does not enter the gases leaving the tower in the first tower. |
| format | Article |
| id | doaj-art-d75d006981e645428cf4a06cc6cbc32e |
| institution | Kabale University |
| issn | 2008-4854 2783-2538 |
| language | fas |
| publishDate | 2024-12-01 |
| publisher | Semnan University |
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| series | مجله مدل سازی در مهندسی |
| spelling | doaj-art-d75d006981e645428cf4a06cc6cbc32e2025-01-15T08:17:35ZfasSemnan Universityمجله مدل سازی در مهندسی2008-48542783-25382024-12-012279597710.22075/jme.2024.32113.25479174Simulation of Sour Water Stripping Unit in Oil Refinery with Consideration of Ammonia SeparationHassan Shahidi0Mehrab Fallahi1Department of Chemical Engineering, Ahar Branch, Islamic Azad University, Ahar, IranDepartment of Chemical Engineering, Ahar Branch, Islamic Azad University, Ahar, IranIn this research, the sour water unit and its simulation were investigated. Sour water unit of refineries usually has two stripping towers in series. The results of this study showed that with the increase in the volumetric flow rate of the incoming sour water feed, the molar flow of NH3 in the exit gases from the first tower increases. With increasing feed temperature, the NH3 and H2S do not change much until the temperature of 1050C, and after that, the relative molarity of these two substances in the exhaust gases decreases with increasing temperature. By increasing the reflux to the first tower to about 9 m3/hr, the molar flow rate of NH3 gas in the first tower decreases drastically, which actually increases the purity of H2S in the exit gases of this tower and increases the flow of this component in the exit gases from the second tower. Also, with the increase in the temperature of the end of the tower, the flow of NH3 and H2S increases and at a temperature of about 120 0C, all the H2S in the feed enters the exit gases from the first tower and the exit water from the first tower is free of H2S. As a result, it can be concluded that the best temperature for the bottom of the first tower is about 120 0C so that all the H2S is removed from the water and NH3 does not enter the gases leaving the tower in the first tower.https://modelling.semnan.ac.ir/article_9174_9bf3c51e3ab2ac727fecf1ff53dabfd9.pdfsimulationsour waterhydrogen sulfideammoniaoil refinery |
| spellingShingle | Hassan Shahidi Mehrab Fallahi Simulation of Sour Water Stripping Unit in Oil Refinery with Consideration of Ammonia Separation مجله مدل سازی در مهندسی simulation sour water hydrogen sulfide ammonia oil refinery |
| title | Simulation of Sour Water Stripping Unit in Oil Refinery with Consideration of Ammonia Separation |
| title_full | Simulation of Sour Water Stripping Unit in Oil Refinery with Consideration of Ammonia Separation |
| title_fullStr | Simulation of Sour Water Stripping Unit in Oil Refinery with Consideration of Ammonia Separation |
| title_full_unstemmed | Simulation of Sour Water Stripping Unit in Oil Refinery with Consideration of Ammonia Separation |
| title_short | Simulation of Sour Water Stripping Unit in Oil Refinery with Consideration of Ammonia Separation |
| title_sort | simulation of sour water stripping unit in oil refinery with consideration of ammonia separation |
| topic | simulation sour water hydrogen sulfide ammonia oil refinery |
| url | https://modelling.semnan.ac.ir/article_9174_9bf3c51e3ab2ac727fecf1ff53dabfd9.pdf |
| work_keys_str_mv | AT hassanshahidi simulationofsourwaterstrippingunitinoilrefinerywithconsiderationofammoniaseparation AT mehrabfallahi simulationofsourwaterstrippingunitinoilrefinerywithconsiderationofammoniaseparation |