【JST-010】One-on-one Q&A Office for Hydrogen Production, Hydroprocessing, and Reforming Unit Processes
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This post was last edited by Firefly on 2015-4-10 08:18. To better share knowledge and skills with everyone and as a challenge for myself, a dedicated Q&A thread has been created. My expertise includes hydrogenation refining of gasoline and diesel, hydrogenation reforming of diesel, operations related to dry gas and natural gas, as well as accident handling in hydrogen production processes. Work experience: Responsible for the initial commissioning and process management of multiple dry gas hydrogen production units, gasoline and diesel hydrorefining units, as well as diesel hydroprocessing units. It’s not design work. I will do my best to answer any questions raised. Note: 1) This post mainly discusses issues related to the hydroprocessing of gasoline and diesel, diesel upgrading, hydrogen production from dry gas, hydrogen production without pre-conversion, as well as the operational procedures and accident analysis of PSA units, with the aim of exchanging ideas and improving together. 2) This post is intended for one-on-one discussions between those seeking help and me; other forum users are also welcome to participate in the discussions. If you are not satisfied with the responses, please create a new thread in the Hydrogen Production and Hydrogenation Technology forum. Thank you for your cooperation! 3) Due to work commitments, I may not be able to respond promptly; please understand!
Teacher shiyue528, I would like to ask a question first. I’ve just started working with light oil hydrogenation, and I’m not quite sure whether water or steam should be used to deal with light oil leaks. Could you please explain this?
There are many different situations; processing can be carried out without stopping operations: if there is only a slight leak, it’s possible to seal it while the system is under pressure, with steam used to provide protection during this process. Actions required to halt operations: steam shielding of the leak, cooling, removal of oil, and using water to displace the oil. Re-vapor purge. There are other situations as well, such as leaks in areas with high temperatures or at normal temperatures; each case needs to be analyzed on its own. The general steps are to cool down, remove oil, and use water to displace the oil. Steam line cleaning. Water on top of the oil reaches the tank area, so steam cannot be used to enter the tanks. Piping purging is done using steam. It goes into the dirty oil tank, with the vapor phase going to the low-voltage section.
Teacher shiyue528, I also have a question: what is the most important indicator for representing the hydrogen consumption amount in hydroprocessing feedstocks?
I’m not sure if the amount of new hydrogen added is correct; previously, we used the amount of new hydrogen added to determine hydrogen consumption! The problems faced by technical teams are all so technically complex. :Q
Can the pressure difference from high to low pressure in the 600,000-ton hydroprocessing of gasoline and diesel mixtures be used to drive a feedwater pump via a turbine? If so, what would the investment cost be approximately?
The last edit to this post was made by shiyue528 on 2014-3-27 at 17:17. Hydrogen consumption in hydrogenation mainly occurs during reactions such as the removal of sulfur, nitrogen, oxygen, olefins, and aromatics from the feedstock, as well as saturation reactions, cracking, and ring-opening reactions. Different reaction processes, varying chemical compositions of the raw materials, and different quality requirements for the products all lead to different reaction severity levels; these are the main factors that affect the hydrogen consumption in hydrogenation reactions. The most important indicators that can reflect the amount of hydrogen consumed are the content of unsaturated hydrocarbons (bromine value), as well as the contents of sulfur, nitrogen, and oxygen. I lack knowledge in theoretical aspects; if there are any mistakes, please feel free to point them out.
Turbo belt feed pumps generally come equipped with a feed pump; I have not encountered any that come with a dedicated feed pump. I have learned that in many cases, turbines fail to operate properly, resulting in low pressure and a small pressure difference. One of our modification units processes over 100 kilograms of material; the turbine operates normally there. The other unit is used for refining, with a pressure of 80 kilograms, but the turbine fails to start up. You can consult the manufacturer specifically and ask them to do the calculations. Our feed pump with turbine costs over 2 million. The injection pump also costs over 2 million.
Diesel hydrogenation: I saw a unit some time ago that used hydrogen mixing both in front of and behind the furnace. I would like to know what the advantages and disadvantages are of this design approach compared to using hydrogen mixing only in front of or behind the furnace
This post was last edited by shiyue528 on 2014-3-28 at 10:48. You can take a look at these posts; the answers provided are quite comprehensive: http://bbs.hcbbs.com/thread-461076-1-1.html http://bbs.hcbbs.com/thread-228648-1-1.html
Why isn’t diesel upgrading referred to as diesel hydroprocessing, just like gasoline hydroprocessing? Thank you