In the video the towers are misnamed the De-propaniser is column 6 the columns marked 2 is the C3 splitter which is one tower spilt into two as it isn't practical to build one tower. Column 4 is the DeMethaniser pre stripper, fitted in order to rebottleneck the plant in the 1980's. Column 5 is the De-Methanizer, 3 is the C2 splitter, Column 1 is the secondary De-ethaniser, I worked on that plant as an Instrument Tech and Control room operator from 1979(commissioning) and 2018.
Errr as an ex-control room operator on that very plant for 43 years, Olefins 6 Plant originally ICI's Kellogg design now run by Sabic. You have the towers mixed up, the tower numbered 6 is the Depropaniser removing C3 from the C4&5 stream, 4&5 are the De-Methanizer's removing the C1 from the C2, 3 is correctly the C2 Splitter removing the Ethane from the Ethylene, 2 are the C3 Splitters removing any remaining Propane and C4 from the Propylene, 1 correctly is the Debutaniser but it is removing the C4 from the C5.NOT the C1 and C3 streams, C1 isn't part of the C3 stream it is removed as part of the C1&C2 stream.C1=Methane is lighter than C2 Ethane/Ethylene and is much lighter than C3 so is part of the Cold Fractionation stream. C3,4,5 are part of the Warm Fractionation stream. Sorry for being pedantic but it sounded wrong......
thanks for explaining this process and awesome way to describe different ways to crack ethane! i currently work in petrochemical company as a fire fighter and our company uses the steam crack way to extract ethylene. i wonder what should i be worry about this process and what are the hazards and the most dangerous parts of this process i mean (furnace, tank, compressor and etc ) ! it would be vary useful for me and our fire department because we risk our lives there and we need to be fully aware of the hazards of this process . tnx again
Hey Mehr, thanks for your feedback and comment! Well.. there are many issues, truly, the main unit is typically well guarded with many security/hazards prevention. The sub-units, or all the other units working behind the main unit are the ones that should be paid extra attention.
This is a great presentation. Would youhave a recommendation for a easly to follow diagram that would illustrate how these many different products you list are created through the cracking process. I am trying to help explain the complexity of the ghg lifecycle analysis challenge when allocating emissions to processes generating multiple chemistries at different points.
Hi! Sure, you can check this content on the course. Regarding Emissions, its a great idea, I'll try to add some information on that in an upcoming course on Environment + O&G
yeah, that is the very broad idea, once you get to separate it, you will see that it is not that easy to separate them as that, specially because you will spend much more in cooling/heating and pumping/compressing due to the mass transfer drive force being "small"... what you want is to spend the least amount of energy as possible. In summary, your approach is correct overall, but will cost a lot $$
The separation train went, C1 split from the C2's in the DeEthaniser, the C2's then went onwards to Hydrogenation and then C2 Splitter so that any Ethane and residual Methane was removed. The C3-5&6 was extracted as a bottom take off of the Final stage Compresion chain. C3 was taken overhead from the DePropaniser, the base cut was then taken to the Secondary DePropaniser to split the C4 from the C5. The Depropaniser overheads was directed to a Hydrogenator to remove the C3 Acetylenes, then to the Secondary DeEthaniser to remove residual Hydrogen, this was then sent to the C3 splitter to remove any residual Acetylenes. The Aim was to produce C2, C3, C4 (ButylButelenes). Also the Hydrogen and Methane was removed in the initial stages...This was the Kellogg designed Olefins 6 Cracker at Wilton on Teesside I was part of the commissioning in 1979 and left in 2018 just before it closed down.
It’s ethane/propane gas. If you look at every olefin plant built in the last decade you’ll notice they are built to ONLY crack natural gas feeds for the most part. Naphtha and other liquid feeds are not used nearly as much as they used to be.
Hi! I recently subscribed to your channel, it has been very helpful so far. I was looking for polyethylene production processes, do you have something posted about it? Thank you!
Hi there! thanks Maria... unfortunately, I havent cover any material on polymerization... but will do in the future... check out my courses for basic petrochemicals, in which we talk about ethylene production =)
Very great video! Thanks for making it. I am wondering why is steam used for the cracking? Couldn't the naphtha be cracked to olefins by just using a zeolite catalyst and inert gas (nitrogen)?
Off the top of my head, we used Naphtha and Propane, feed rates were usually around 30Tes/Hr, with a radiant coil outlet temp of around 900 deg C. Usually there were at least 15 furnaces in operation, which produced 100 Tes/He C2 and 45 Tes/Hr C3. As well as the C4 make and C5-6's, Hydrogen and Methane was chilled out for use in the Hydrogenation reactors and the Methane went to Fuel Gas for the Furnaces. The residual heat from the furnaces was used to produce VHP steam and let down and superheated to produce steam for the compressors . A Caustic Scrubber was used to remove the CO2 and H2S acid gasses between the third and fourth stage of process gas compression, the catalyst used in the hydrogenation train was poisoned by these otherwise. Every form of residual heat was used on the complex to produce some other 'work' so nothing was wasted in theory...The mass balance calculation was truly a sight to behold and was produced using 'magic' as far as I could tell...feel free to contact me for more anecdotal tales...
In all the olefins plants I have worked in and that I have seen, the C2 splitter is usually the tallest and widest column in the unit.
In the video the towers are misnamed the De-propaniser is column 6 the columns marked 2 is the C3 splitter which is one tower spilt into two as it isn't practical to build one tower. Column 4 is the DeMethaniser pre stripper, fitted in order to rebottleneck the plant in the 1980's. Column 5 is the De-Methanizer, 3 is the C2 splitter, Column 1 is the secondary De-ethaniser, I worked on that plant as an Instrument Tech and Control room operator from 1979(commissioning) and 2018.
Errr as an ex-control room operator on that very plant for 43 years, Olefins 6 Plant originally ICI's Kellogg design now run by Sabic. You have the towers mixed up, the tower numbered 6 is the Depropaniser removing C3 from the C4&5 stream, 4&5 are the De-Methanizer's removing the C1 from the C2, 3 is correctly the C2 Splitter removing the Ethane from the Ethylene, 2 are the C3 Splitters removing any remaining Propane and C4 from the Propylene, 1 correctly is the Debutaniser but it is removing the C4 from the C5.NOT the C1 and C3 streams, C1 isn't part of the C3 stream it is removed as part of the C1&C2 stream.C1=Methane is lighter than C2 Ethane/Ethylene and is much lighter than C3 so is part of the Cold Fractionation stream. C3,4,5 are part of the Warm Fractionation stream. Sorry for being pedantic but it sounded wrong......
Hey thanks for getting in touch! Make no worries on pedantic, It really helps!
@@ChemicalEngineeringGuy Any time just e-mail me if you want practical anecdotal evidence for your classes.....
thanks for explaining this process and awesome way to describe different ways to crack ethane! i currently work in petrochemical company as a fire fighter and our company uses the steam crack way to extract ethylene. i wonder what should i be worry about this process and what are the hazards and the most dangerous parts of this process i mean (furnace, tank, compressor and etc ) ! it would be vary useful for me and our fire department because we risk our lives there and we need to be fully aware of the hazards of this process . tnx again
Hey Mehr, thanks for your feedback and comment! Well.. there are many issues, truly, the main unit is typically well guarded with many security/hazards prevention. The sub-units, or all the other units working behind the main unit are the ones that should be paid extra attention.
This is a great presentation. Would youhave a recommendation for a easly to follow diagram that would illustrate how these many different products you list are created through the cracking process. I am trying to help explain the complexity of the ghg lifecycle analysis challenge when allocating emissions to processes generating multiple chemistries at different points.
Hi! Sure, you can check this content on the course. Regarding Emissions, its a great idea, I'll try to add some information on that in an upcoming course on Environment + O&G
I think you should separate c1 first, then c2 and c3 and c4. Because weights are: c1 < c2 < c3 < c4.
yeah, that is the very broad idea, once you get to separate it, you will see that it is not that easy to separate them as that, specially because you will spend much more in cooling/heating and pumping/compressing due to the mass transfer drive force being "small"... what you want is to spend the least amount of energy as possible. In summary, your approach is correct overall, but will cost a lot $$
The separation train went, C1 split from the C2's in the DeEthaniser, the C2's then went onwards to Hydrogenation and then C2 Splitter so that any Ethane and residual Methane was removed. The C3-5&6 was extracted as a bottom take off of the Final stage Compresion chain. C3 was taken overhead from the DePropaniser, the base cut was then taken to the Secondary DePropaniser to split the C4 from the C5. The Depropaniser overheads was directed to a Hydrogenator to remove the C3 Acetylenes, then to the Secondary DeEthaniser to remove residual Hydrogen, this was then sent to the C3 splitter to remove any residual Acetylenes. The Aim was to produce C2, C3, C4 (ButylButelenes). Also the Hydrogen and Methane was removed in the initial stages...This was the Kellogg designed Olefins 6 Cracker at Wilton on Teesside I was part of the commissioning in 1979 and left in 2018 just before it closed down.
I have a question, what would be the best feedstock in producing ethylene and propylene via steam cracking?
a very rich olefin naptha will do great :)
It’s ethane/propane gas. If you look at every olefin plant built in the last decade you’ll notice they are built to ONLY crack natural gas feeds for the most part. Naphtha and other liquid feeds are not used nearly as much as they used to be.
Hello there😃, for 0:20 is there any reference or journal articles, because it will be helpful for my research
Well, I wrote an article on that www.aiche.org/resources/publications/cep/2021/october/overview-hydrotreating
@@ChemicalEngineeringGuy Thank you so much 🙏
Hi! I recently subscribed to your channel, it has been very helpful so far. I was looking for polyethylene production processes, do you have something posted about it? Thank you!
Hi there! thanks Maria... unfortunately, I havent cover any material on polymerization... but will do in the future... check out my courses for basic petrochemicals, in which we talk about ethylene production =)
Very great video! Thanks for making it. I am wondering why is steam used for the cracking? Couldn't the naphtha be cracked to olefins by just using a zeolite catalyst and inert gas (nitrogen)?
YES! they can, but its way cheaper and efficient with steam
i tought you ment steam cracking on the steam platform...
me too
What is x& y
can we replace the scrubber with adsorption column to deacidification and remove remaining CO2?
yeah, but the process will not be exactly the same. Scrubbers as typically cheaper to get and operate as well
What about the continuing lecturers where can I watch them ?
courses.chemicalengineeringguy.com/courses you can check out the full oil & Gas bundle, or go directly to petrochemical course
What is the approximate specific heat consumption of the pyrolysis reactor (MJ/kg of feed)?
Off the top of my head, we used Naphtha and Propane, feed rates were usually around 30Tes/Hr, with a radiant coil outlet temp of around 900 deg C. Usually there were at least 15 furnaces in operation, which produced 100 Tes/He C2 and 45 Tes/Hr C3. As well as the C4 make and C5-6's, Hydrogen and Methane was chilled out for use in the Hydrogenation reactors and the Methane went to Fuel Gas for the Furnaces. The residual heat from the furnaces was used to produce VHP steam and let down and superheated to produce steam for the compressors . A Caustic Scrubber was used to remove the CO2 and H2S acid gasses between the third and fourth stage of process gas compression, the catalyst used in the hydrogenation train was poisoned by these otherwise. Every form of residual heat was used on the complex to produce some other 'work' so nothing was wasted in theory...The mass balance calculation was truly a sight to behold and was produced using 'magic' as far as I could tell...feel free to contact me for more anecdotal tales...
wow! thanks for jumpin in! great input
@@ChemicalEngineeringGuy any time, I'm retired but can recall most of the operational side...
where the rotating disc is used in which stage??
Sorry, what especific minute of the lecture are you alking about?
can you post about naphtha cracking in furnace system?
Those are included in the full course, check it on my website
Can you suggest a certification course for Petrochemical engineer
check this out: courses.chemicalengineeringguy.com/courses/category/oil%20&%20gas