【JST-074】Container, Heat Exchanger Technical Discussion One-on-One Office
Thread Content
This post was last edited by Firefly on 2015-4-10 at 08:51. I hope to learn together with fellow enthusiasts and improve together. Online hours: Monday to Friday, 12:00–13:30; I may also be online at other times – you can contact me via QQ: 958471176. My area of expertise includes design-related issues related to containers and heat exchangers, as well as structural design and strength calculation problems; we can discuss these topics together. Note: The purpose is primarily mutual learning; it’s best to discuss practical design problems, as well as issues encountered in production sites. Moderator’s note: This post is intended for technical discussions between Feitianxue and fellow enthusiasts only; please refrain from participating in the discussion. If you have any objections, please post a new thread in the Container and Storage Equipment forum for discussion. Thank you for your cooperation! ) Bubu Spin
In-depth analysis of hydrochloric acid: How to design analysis towers
Your question is a bit too broad. Could you be more specific? I’m not yet clear what you mean by \"design\" – does it refer to process calculations, or something related to equipment structure? Please be more specific.
This post was last edited by yuchenchf on 2012-4-4 09:11. Which is more effective for absorption – packing absorption or falling film absorption – for the absorption of hydrogen chloride? (Forum moderator’s tip: Refer to answer on floor 6.)
There is also a detailed explanation in hydrochloric acid regarding how to design distillation towers
This issue is mainly a process-related problem, that is, the preliminary calculations for the equipment; it pertains to process estimation, equipment selection (such as determining the equipment diameter and height), as well as the process parameters and methods (such as the packing height and type of packing)； I don’t know much about this, so I don’t dare to speak rashly ； I hope to post this question in the Process section or the Tower Equipment section to consult with relevant experts ； If issues arise regarding strength or other internal structural designs during the calculation of the device, we can discuss them together.
Okay, thank you so much again
This post was last edited by yuchenchf on 2012-4-4 09:11. The area indicated on the heat exchanger’s nameplate differs slightly from the area calculated based on the tubes (with the portion extending into the tube sheet taken into account using a formula). It also sometimes differs from the area listed for that heat exchanger series (is this similar to the nominal diameter?). I posted this question before, and others provided some brief responses, but they weren’t very clear. Please give a clear explanation, thank you. (Publisher’s note: Refer to answer on floor 9 for guidance.)
The area indicated on the nameplate of a typical heat exchanger should be the same as the area shown in the actual drawings, which is related to the factors taken into consideration by the actual designers； The area listed in the heat exchanger series is a reference value and does not represent the actual area of the heat exchanger; this is because the area of a heat exchanger depends on the thickness of the tube sheet as well as on its specific structural design ； For example, in the case of shell-and-tube U-shaped tube heat exchangers, when performing specific calculations, the area of the bent sections must also be taken into account, as this area is also involved in the heat exchange process ； Some designers fail to include this portion of the heat exchange area, which does not correspond to reality. In a regular U-tube heat exchanger, the area of the bent sections is not taken into account ； Therefore, the specific heat exchanger area should be treated on a case-by-case basis, with the design drawings being the primary reference.
This post was last edited by yuchenchf on 2012-4-4 09:12. Teacher, I have a question regarding the external pressure verification for heat exchangers; thank you for your help! 1. Is it necessary to perform an external pressure check for each heat exchanger during calculation? 2. Under what circumstances is external pressure verification not required? 3. For example, under the current design conditions: shell side pressure is 0.8 MPa at 250°, while the tube side pressure is -0.1 MPa at 100°; the material used is Q245R. Normally, when entering the data for the heat exchanger, the values are set as 0.8 for the shell side and -0.1 for the tube side. Now, is it necessary to verify the values as shell side -0.1 and tube side -0.1? (A former colleague said that since the shells are the same, there’s no need for compensation; I don’t understand this.) 4. Additionally, in the case of vertical fixed-tube plate heat exchangers, has the weight of the heat exchange tubes and the medium they carry already been taken into account in the SW6 calculations? What are the differences between the upper and lower tube sheets? ? (Moderator’s tip: Refer to answer on floor 13)
The hydrochloric acid separation does not necessarily require a separation tower; a simple stripping section is sufficient, and a distillation unit is not needed, as that would result in higher investment costs.