It's not finished yet. A lot still to be done

Just ask your questions here

Hi, let me see if I can find any information for that. If you already have any, just send them to me so that we can quickly start

@@ZulfanAdiPutra Can you please share with me your email address? Thanks a lot

Hi, I don't have any case study for that. If you have any, let's dig into that

1. HYSYS bisa menghitung apapun yg kita bisa modelkan. Pertanyaannya adalah apakah kita mengerti sistem yg kita mau modelkan dan apakah kita bisa memodelkannya? 2. Buat apa memodelkan sistem spt itu? Apa yg mau dicari? 3. Di contoh ini keliatan bahwa pressure gabungannya berubah tergantung dari tekanan kedua vessel tsb.

Bisa

Biar lancar nanti 😊

Hi, I don't have the process. If you have it, please share it :)

No need man

Masih lama Mas. Masih harus di-massage lagi. Sabar, hehehe...

Bentar saya mau upload v0.0.2 nya, hehehe... Stay tune

Memang gak ada. Ini saya buat sendiri pake custom GPT

Hi, thanks for the comment. It is unfortunately not available. Sorry

Hi, thanks for the comment. I am not sure what happens at your end, but it looks fine from my end. I can "like" and "share" this video. Could you please try it again.

Hi, do you want to see a slower simulation in your pc or something else? :) If it is the first, then you can tick "real time" in the Integrator or if it feels so slow because of this, you can then set the acceleration in the Integrator to a value bigger than 1. The effect of flow control is relatively fast because its "capacity" is only the volume from the flow measurement and the flow control valve itself. So, it is a very small volume (relative to others). Hence, relatively quick response. IF, your pipe is big and the distance between the flow measurement and the control valve is like 1 km or more :), then you'll see a much slower response. This is what we see as "dead time". When controlling a process, we typically want to have the system under control as fast as we can. Not the other way around.

Thank you so much.

Hi, thanks! I think you can check out my playlist for Aspen HYSYS where few dynamic simulation videos are available: kzbin.info/aero/PLFK7DKgtefxsqVDL5bLMzQYP-Cy4DenW5

silahkeun

Thanks man

Ada. Ayo gabung di grup telegram Teknik Kimia Indonesia

permisi, yang mana ya pak ada link nya kah?@@ZulfanAdiPutra

Mantap

Kalo kita plot profil temperatur terhadap tray dan kita dapati temperaturnya ga berubah, berarti ga terjadi proses pemisahan di tray2 tsb. Artinya, tray2 yg temperaturnya ga berubah ini bisa dibuang

@@ZulfanAdiPutra terima kasih pak Zulfan

Hi, I don't know if there is. To do dynamic simulation in Aspen PLUS is not as user friendly as in HYSYS.

Hi, unfortunately not. This is one of the courses in MSc in Process Integration at UTP

Hi, unfortunately there is no such course at the moment. This one was part of an MSc program, called Process Integration, at UTP.

Hi, there is no such course at the moment.

Hi, thanks for the comment. Yes indeed, I'm planning to do so. Thanks again for the suggestion

@@ZulfanAdiPutra hi, thanks for the answer. Could you please refer me any literature that can guide me about optimization modeling of chemical engineering problems, specifically process synthesis. Thanks

​@@SyedHaider-x7t hi, you can refer to Optimization of Chemical Processes, Systematic Methods of Chemical Process Design, or even Advanced Optimization for Process Systems Engineering

Hi Tan, you are right and you can include it if you want. This simple simulation is only to provide a basis on how to make a temperature control. Of course you can always add more complexities into the system. Just please be careful to always understand what you want to simulate and why you make such choices

@@ZulfanAdiPutra alright i have understood the context. Thanks for your kind explanations!

You can use HYSYS to calculate CV for you. Check in the sizing tab. It's basically a straightforward calculation using flowrate and dp that you allow for

😂

Thanks. It was run using the default solver: Interior Point.

Sorry, are you asking for the name of the software? It's Symmetry from SLB.

Thanks. You can simply google it. There are many

well, you can see the intersection relative to the limits. If you go to the hydraulic plot (typically shown next to the column), in the tab "Internal", click view in the section that you want to see, you'll see a pop-up window of "Geometry". In its "Results" tab, you can select to see "By Tray" and you'll see the flooding percentages per tray. I hope you can find it.

Hi, I am not aware of any printed material explaining this issue in depth. It's basically as simple as what I explain in the video. We need to balancw the supervicial velocity of vapor and liquid and these numbers need to be located about in the middle for convenient. If we have too high vapor velocity, it will go up in the graph and we'll get entrainment in the end. If the vapor velocity is too low, it will go down in the graph, and we'll get weeping from the trays. Obviously, the shape of the graph highly depends on the properties of the vapor and liquid (ie thermodynamic estimation must be accurate enough), the vapor and liquid load (ie capacity), the diameter of the tray, and the type and the design of the tray itself. So, you can play around with all these parameters and see how the plot changes, and how the vapor-liquid intersection moves in the plot

@@ZulfanAdiPutra Thank you very much. I'll will do exactly as you have said. I appreciate

Am I welcome to ask more questions as I proceed with my design project?

@@isotuadonye303 you can always ask questions

@@ZulfanAdiPutra In my design. The column consists of 10 trays (sieve). I'm told that the liquid rate is less than the minimum weir loading rate specified. While tray 6-10 is experiencing weeping. Please what can I do?

Hi, you can find Symmetry tutorial for dynamic simulation in my channel. Both are basically the same for the functionality and ease of use. There are some minor differences, eg valve opening 0-100% or 0-1. For stability, I have encountered 2 occasions where I have to remove and re-add some unit operations in HYSYS.

This one and the next one kzbin.info/www/bejne/qGKaY2qhnbuSZ7M

@@ZulfanAdiPutra Awesome! Thank you once again!

Sama2

Hi, We typically use cascade control if we have more than 1 measurements (in the example above they are level and flow measurements) AND 1 final control element (which is the flow control valve). Another point as a rule of thumb is that the inner loop (slave) has to be a lot faster than the outer loop (master). It's of course more complicated than a single control loop. However, if we can justify the benefits of using the cascade mode, it's worth it. For example: 1. Reflux is typically done by using the reflux flowrate as the measured variable and we have the set point for it. When feed flowrate or composition changes, this reflux flowrate has to be changed accordingly. But, to how much extent? Well, we can do trial and errors for that. Or, if we can have a composition measurement on the distillate stream, which you know it is much much slower than measuring the flowrate of the reflux, we can use this composition measurement to tell what the reflux flowrate should be. Thus, the composition control loop is the master and the reflux flowrate is the slave. 2. In heat exchanger where we heat a process stream with a steam, we can have two measurements, which are flowrate of the steam and the process outlet temperature. And we know that changing the opening of the steam control valve will change the steam flowrate much faster than the process outlet temperature. Thus, we can use the process outlet temperature control loop as the master and the steam flowrate control loop as the slave. We could of course neglect the flowrate measurement of the steam by directly manipulating the steam flowrate from the process outlet temperature (aka controlling steam flowrate without knowing how much it is flowing). But, we almost always have steam flowrate measurements for energy balance and others. When we have disturbances for these two examples such as changing feed compositions (ex. 1) or changing steam pressure (ex. 2), this cascade control can bring some stabilities to the performance. You can simulate this and compare the result with the simple control. By the way, the example in the video that you referred to is not a really good example to explain the benefit of cascade against a simple control loop as you have discovered. So, well done! Nonetheless, it may have been that the level is a more important variable to control than the flowrate. Thus, it needs to be measured and becomes the master.

@@ZulfanAdiPutra That's a very detailed explanation and it makes a whole lot of sense. Thank you so much!

Thanks a lot

Thanks. Glad you like it

Thanks a lot

Terima kasih banyak

Thanks. Unfortunately, I don't remember where that file is stored :(