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Thank you for the knowledge & I learned something new today! Please note that the pv2 values in the calculated spreadsheet and Aspen Plus vary slightly due to differences in the fluid composition used for C2+, which results in different mass densities. This is crucial for estimating the vibration effect on the fluid flowing in the pipe. In real work, it's best to obtain the complete fluid characterization for heavy hydrocarbons as well to closely match their properties to the sizing results. However, for a percent difference of less than 5%, the simulation result is acceptable in this case. Just my two cents

Hats Off to trainer Mohamadreza Sir!

how do you know relieving temp??

Very helpful content. Thanks for sharing

Can anyone say what are the changes we need to do if we have a phase change in one stream? Even though i have change in flash options of the streams, still in EDR console it doesn't work

Thank you so much for your explanation . My question is on the pipe entrance K factor. From Crane 410, Page A29 the value of K depends on the r/d where r is the bending radius and d is the ID of the pipe. K values are provided for r/d= 0.0 ,0.02,0.04,0.06,0.01, 0.15 &up. I observed K value 0.5 for r/d =0.0 was used in the example. Please how was the value calculated. I am having challenges on how to get the bending radius r.

How do we calculate the mass relief flow ???

Thank you Mr. Behroozi excellent work for Inst Engg

Thanks for the informative vedio I believe we can't say it's a process designer rather than equipment failure

Your explanation is baseless without an answer. What did you arrive at? What size of rupture disc for a said pressure vessel? Unfortunately, you didn't satisfy the aim of your calculations

Can you please guid me,how I can see 5 hidden videos on psvs, now I can see only 2 videos out of seven. Thanks.

I too can't find the htri tutorial which was available earlier. Sir whether it has been removed.

@EIEPD PLEASE UPLOAD PSV SIZING FOR WETTED AND UNWETTED SURFACE

HI Sir which standard are you using for sizing the line

can i know what standard u use in design criteria?

please share the HE design by HTRI also..

عالی

dear sir please reupload htri videos

When I checked exida’s channel video I saw that Route2h table is different than yours since if HFT=0 then SIL shall be 1 as per your video but if HFT=0 then SIL shall be 2 as per exida’s video. Do you think that which is true? (1:30:42)

Hi, Thanks for good presentation, how can we have relevant PDF file?

Hi dr Continue with power Grateful

Please reupload the htri vedios

Thank you for your video. However, I think you made some mistakes in addressing the main reason for the trip. You should know that the suction pressure of the ID Fan is not the cause of the reformer trip (IS-1). Furnace draft pressure (that is one of the causes of IS-1 trip) is different from ID fan suction pressure (i.e. PIC-2224 is the cause of IS-1 not PI-2156 in your plant). I think the main reason for the trip was the fluctuation in the temperature and flow rate of the combustion air. As the site operator had opened the bypass of E-2007, the combustion air temperature decreased, and as a result, its flow rate decreased. A decrease in combustion air flow rate leads to more vacuum in the furnace and can trigger IS-1 trip. Thank you again for sharing your valuable experience and hope my comment will be helpful.

Tremendous work team EIEPD Well done Keep Educating a preciou content

it's fantastic Experience at EIEPD content

Hello sir , could you please share the download link of air cooler design

Waiting for upcoming lectures on Aspen software????

I couldn't find the video for HE design by HTIR? It has been removed?

Rather than using the word “Mistake” is better to use “learning”

please advise for latent heat calculation for three phase separator. i mean two different liquid.thanks in adcance

good job mr. behroozi

Many thanks!

Thank you very this course helped me a lot

Thanks a lot!

Really It will helpful, Thanks

From where i get this software

Good explanation but since There is no excelsheet here or on website so the training is not useful

Sir could you please demonstrate these in ASPEN 1.Determination of temperature profiles for heat exchanger 2. Determination of Concentration profiles for reactor

Thank you

thanks for sharing. Enjoyed this presentation

Thank you for sharing

Nice topic, nice presentation. Thank you.

thank you of sharing video. Very helpful.

In our deaerators we have LV installed wich cotrol the excess of level and overflow, it discharges to drain header, it has a big line size, we call it in french 'vanne trop plein'

Greatest application of aspen plus ive seen! thanks sir. very helpful

Nice videos, thank bro

Thank you sir, i will keep that in mind.

Can I modify shell and tube HX as a reactor in Aspen Plus?

Nice