17- Solutions for expanding the capacity of power plant steam boilers by utilizing the existing flue gas desulfurization scrubber demister and dust remover
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This post was last edited by luoli519 on 2023-10-3 at 16:36. Recently, a certain thermoelectric company upgraded its existing steam boilers significantly, which resulted in the flue gas output from these boilers increasing by three times compared to before. Given the existing site constraints and investment considerations, the company intends to build on the existing flue gas desulfurization scrubbers and seek competitive proposals from specialized desulfurization solution providers that meet the requirements for compliant emissions. By retaining the existing desulfurization washing and absorption tower, the flow velocity of the boiler flue gas at the original tower diameter increases to three times after the capacity expansion. Optimizing the design and increasing the spraying density of the desulfurization liquid can achieve the desulfurization goal. However, the foam and mist removal solutions for flue gas at high gas velocities face challenges. Whether using the currently mainstream domestic and international flat (FLAT) blade arrangement scheme or the ridge (ROOF) blade arrangement scheme, the normal flow velocity of the smoke over the blades far exceeds the upper operating limit required to meet the demisting requirements. I hope fellow sailors can help come up with some ideas and discuss whether there are any better foam removal methods
This post was last edited by luoli519 on 2023-10-3 at 16:38. Additionally, the following professional discussion posts that I posted on the Haichuan Chemical Industry Forum are listed here for everyone to use as links to join the discussions: 13. Discussion on improvements to the inlet devices of cyclone separators in gas-solid separation applications; please visit http://bbs.hcbbs.com/thread-1614524-1-1.html to participate in the discussion. 14. Regarding the issues arising from the use of swirl tube/swirl plate demisters in the wet flue gas desulfurization process for boilers, please visit http://bbs.hcbbs.com/thread-1599605-1-1.html to participate in the discussion.
This post was last edited by luoli519 on 2023-10-3 at 16:38. 35. Discussion on the removal of liquid sulfur foam from SO2 in the sulfur dioxide production unit of the sulfolane plant: http://bbs.hcbbs.com/thread-1616252-1-1.html.
37. Regarding the application of the C4 hydrocarbons/water coalescing separator in the MMA methyl methacrylate project, please visit http://bbs.hcbbs.com/thread-1617142-1-1.html to participate in the discussion. To be continued......
This post was last edited by luoli519 on 2023-10-3 at 16:38. For discussions on measures to remove liquid droplets from the flue gas resulting from the mixed combustion of waste gas from chlor-alkali plants and coke oven gas, as well as related heat recovery and cooling processes, please visit http://bbs.hcbbs.com/thread-1617257-1-1.html.
40. Regarding the unstable operation of the alcohol synthesis unit in the **installation and the waste alkali liquid separator, which leads to problems in the operation of the subsequent coagulation separator, please visit http://bbs.hcbbs.com/thread-1620515-1-1.html to participate in the discussion. To be continued......
Warning: Please do not post the same content in these 5 posts you have posted; otherwise, it will be treated as spam. Appendix: The 5 posts are as follows: 1. Discussion on the installation of vane-type high-efficiency demisting and deodorizing separators in the vacuum pump exhaust system of the sulfolane plant’s distillation unit. 2. Bag filtration and electrostatic precipitators for flue gas treatment in waste salt and waste alkali incinerators, followed by a multi-factor swirl-type primary and secondary dust collector – NOVE. 3. Severe ammonia nitrogen contamination caused by ammonium droplets carried in the secondary steam from the multi-effect evaporation crystallizers used in the caprolactam plant’s sulfuric acid and hydrochloric acid mixed acid process. 4. Exchange of experiences regarding the selection, design, installation, operation, and maintenance of demisting systems in power plant desulfurization scrubbers. 5. Solutions for significantly expanding the capacity of power plant steam boilers while still using the existing flue gas desulfurization scrubbers – NOVEL Nuwei Energy
Okay, from now on, combine similar reference posts into one of them.
This post was last edited by luoli519 on 2023-10-3 at 16:39. By utilizing the vane-separated internal component technology to change the configuration of these internal components – that is, by using new internal components with a higher upper limit for normal airflow velocity along with their patented configuration techniques – it is possible to handle more than three times the amount of flue gas flow in towers of the original size. Please visit the link https://bbs.hcbbs.com/thread-1354813-1-1.html or log in to www.novelseparationtech.com to learn more about the technical details.
This post was last edited by luoli519 on 2023-10-3 at 16:40. Regarding dynamic separation technology and the design calculations for its components, it should be noted that some manufacturers both domestically and internationally have begun to adopt the vaned separation components produced by NOVEL Company. However, the feather-leaf separation technology is the design result and configuration form derived from the design technology of its precise dynamic separation system platform. It is necessary to rely on the design results and configuration formats obtained through the technology for designing precise kinetic separation system platforms, taking into account fluid dynamics parameters such as the gas phase composition and average molecular weight under different temperature and pressure conditions, the comparative compressibility factor of gases based on air as a reference system, gas phase viscosity, gas phase density, and gas phase flow rate, as well as liquid phase density, liquid phase viscosity, liquid phase surface tension, and the maximum liquid phase flow rate.
With the same operating conditions and process data, the results obtained through calculations and design by non-specialized companies differ significantly from those achieved by professional dynamic separation technology companies using their advanced platforms for precise dynamic separation calculation and design. One of the most significant differences in the design calculations lies in the difference in the gas-phase compressibility factor under their respective operating conditions. It should be noted that precise and reliable dynamic separation technologies and their components must be verified through preliminary model platform experiments. For preliminary model platform testing, the safest and most readily available gaseous medium is air. Therefore, all prior dynamic separation models in the international community are systems using air as the medium. To approximate real operating conditions as closely as possible using a platform model for dynamic separation systems, it is necessary to use the gas phase under real conditions as a reference system similar to air at atmospheric pressure, in order to obtain the compression factor relative to air at atmospheric pressure. This compression factor is very different from the value of the compression factor based on an ideal gas as a reference, as given in the manual! ! The compressibility factor used by non-professional dynamics separation companies is the value of the compressibility factor under ideal conditions as found in handbooks. The volume flow velocity under the operating conditions calculated using this ideal compressibility factor differs significantly from the volume flow velocity through the components of the dynamic separation technology under actual operating conditions. Naturally, there is a significant difference in the separation efficiency achieved at different volumetric flow rates under the same operating conditions! Companies complain that their cyclone separators achieve a separation efficiency far worse than the designed value. Naturally, cyclone separators also belong to dynamic separators. Designing calculations by mistakenly using the compressibility factor of an ideal gas as the relative compressibility factor of air under pseudo-atmospheric pressure is the reason why the actual separation efficiency of cyclone separators manufactured by companies at home and abroad during operation differs significantly from the calculated separation efficiency. In other words, the compression factor from the ideal state specified in the manual was simply copied over; whereas the compression factor used in the parameter conversion related to flow rate in the kinetic separation design model refers to the compression factor based on air under pseudo-atmospheric pressure as a reference system!