【JST-043】One-on-one consultation office for experts in chemical engineering technology and equipment
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This post was last edited by Firefly on 2015-4-10 08:33. Technical discussant, moderator: wiseboy. Major: Chemical Engineering and Technology. My areas of expertise: 1. Fundamental theories of chemical engineering and processes, mathematics of chemical processes, mass transfer processes and equipment, heat transfer processes and equipment, reaction engineering and equipment, chemical thermodynamics and basic data, process simulation, engineering software interface technology ； 2. Information security and smart card hardware encryption technologies for computing software, as well as specialized encryption solutions and implementations for software related to chemical engineering: 1) Software encryption using compilation languages such as VB, VC, Delphi, and FoxPro (with smart card hardware) ； 2) Encryption technologies for special language software such as AutoLisp, VLisp, Excel, etc. (using smart card hardware) ； Daily or weekly online time: 1–2 hours per day from Monday to Friday. Work experience: over 30 years. Everyone is welcome to exchange ideas on theoretical and practical issues in the broad fields of chemical engineering, process industries, and fundamental sciences. (Publisher’s note: Any future requests for information here will be deleted!) I hope everyone makes good use of the opportunity to communicate with experts. ---------Bingbing Spin)
This post was last edited by yuchenchf on 2012-4-4 08:54. Where can I find the isothermal adsorption curves for molecular sieves? Thank you! (Publisher’s note: Refer to answer on floor 3 for guidance.)
This post was last edited by wiseboy on 2012-3-30 17:01, version 1. Generally, the isothermal adsorption curves of molecular sieves are provided by the manufacturers, but they are unreliable. The salesperson didn’t know anything at all when asked questions ； 2. It can be tested and determined. This measurement is not difficult; it can be carried out in universities.
This post was last edited by yuchenchf on 2012-4-4 08:54. Can measurements be taken at temperatures of liquid nitrogen, liquid oxygen, liquid argon, and liquefied natural gas at a pressure of 0.001 Pa? (Publisher’s note: Refer to answer on floor 5 for guidance.)
This post was last edited by wiseboy on 2012-3-30 23:21, version 1. Adsorption in liquids is a bit more complex, but it can be measured. I didn’t understand whether you are referring to adsorption in a liquid or in a gas. Is 0.001 Pa the absolute pressure? 2. The key is to determine the adsorption of that substance, such as the adsorption of H2O in natural gas ； 3. If possible, try to adsorb it in the gaseous state.
This post was last edited by yuchenchf on 2012-4-4 08:55. In chemical process simulation, choosing the appropriate thermodynamic methods presents a challenge; could you recommend some books on selecting thermodynamic methods for simulation software? Thank you! (Publisher’s note: Refer to answer on floor 7 for guidance.)
Selection of thermodynamic methods in simulation software: 1. The help documentation is the best resource ； 2. Other thermodynamics textbooks contain discussions on some of the thermodynamic equations (methods), but keep in mind that simulation software often improves upon the classical thermodynamic equations presented in textbooks; some of these improvements are protected by intellectual property rights, and their details are not made public. Their suitability still needs to be determined by referring to the software’s help documentation. The descriptions in other places will not be more detailed than the help documentation ； 3. The help documentation for simulation software usually includes a dedicated section on “thermodynamic methods”.
This post was last edited by wiseboy on 2012-3-30 23:21, version 1. Adsorption in liquids is a bit more complex, but it can be measured. I didn’t understand whether you are referring to adsorption in a liquid or in a gas. Is 0.001 Pa the absolute pressure? 2. The key is to determine the adsorption of that substance, such as the adsorption of H2O in natural gas ； 3. If possible, try to adsorb it in the gaseous state. What I mean is the adsorption isotherm curve of the molecular sieve used as an adsorbent in the vacuum insulation layer of low-temperature insulated equipment?
This post was last edited by yuchenchf on 2012-4-4 08:55. Hello, I am a recent graduate from 2012 and I’m facing some issues with my graduation project. The topic of my project is the design of a workshop for producing base oils for lubricants; the raw material used is hydrocracking residue oil. The process involves feeding this residue oil into a vacuum distillation unit to remove light components, followed by isomerization and dewaxing, then hydrogenation in series reactors, and finally vacuum distillation to obtain narrow-range fractions. I’m currently doing a material balance calculation, but I’m stuck at the stage of isomerization dewaxing and hydrorefining. When the residue oil enters the isomerization dewaxing reaction, reactions such as nitrogen removal, sulfur removal, and oxygen removal take place. There are so many components in the residue oil – how should I calculate the material balance as well as the amount of hydrogen required? Since S, N, and O are already present in very low amounts in the hydrocracking tail oil, can I roughly consider the reactants entering the isomerization dewaxing reactor to be equal to the products? But then how should the hydrogen consumption be calculated? The question is quite long; thank you for your help! (Publisher’s note: Refer to answer on floor 10 for reference.)
This post was last edited by wiseboy on 2012-4-2 10:29: Changes in composition and molecular weight before and after hydrogenation. However, due to the complex composition of the products, it is difficult to make accurate calculations. You should use the several main reaction equations for hydrogenation, along with their conversion rates, for crop mass balance calculations.
This post was last edited by yuchenchf on 2012-4-4 08:56. Hello: May I ask what the typical heights of the cold hydrogen tray and distributor in a hydrogenation reactor are? The inner diameter of my reactor is 2400 mm, with two catalyst beds; the height of each catalyst bed is 6 m. (Moderator’s note: Refer to answer from floor 12 for guidance.)