Ben Spooner is a great personal with lot of hands on experience and happy to share the knowledge to the resolution permanently. This makes him entirely different. Nice video. Hope in future also will be there opportunity to work again soon.
Thanks for the video, really useful. I had a question. Is there any evidence of increase likelihood of amine SCC on the lean amine circuits when you operate at low amine loading?
Obviously the regeneration rate will be a compromise between the cost of energy use, the downtime caused by exchanger corrosion, and the OPEX for lean amine filter changeouts. Not a straightforward number.
Thank you for the video. I have a question for rich amine corrosion. If rich amine temperature is increased up to 85~90degC , there is corrosion in rich stream especially high pressure process even if rich loading is maintained 0.4~0.45. I know it is affected by amount of H2S flashed. What is a corrosion mechanism? is it similar to form the mackinawite ? If rich loading is enough, the pyrite is already formed.
hi there, as long as the rich loading is composed mostly of H2S (not CO2), and kept below 0.5 mol/mol (or so) there should not be any problems even if the amine is reduced from a high pressure to a low pressure, like across an absorber level control valve for example. The temperature is a concern however, in a typical carbon steel absorber we recommend 85C as the maximum "bulge" temperature to prevent corrosion of the absorber itself. Usually, the rich amine stream is slightly cooler than the bulge temperature - use a simulator to be sure, if you don't have TI's throughout the absorber - so you are putting yourself at risk by operating with 85-90C absorbers. If you have a completely stainless steel absorber, that's different and we routinely see bulge temperatures upwards of 100C.
Thanks for the video, I had a question that is related to the lean/rich exchanger fouling video you did earlier. In this video you state that the high temp - high H2S conditions of the rich amine are good conditions to form the protective iron sulphide layer (pyrite), yet in the previous video, the rich side of the lean/rich exchanger is fouled and the lean side is clean. Why is this the case, it seems to be contradicting with what you say in this video?
Jared, if the rich amine conditions properly form a protective film (pyrrhotite), then you won't have fouling of the rich side of a lean/rich exchanger. The problems are when the conditions are NOT correct for the film formation. This can happen if the rich amine H2S loading is too low, temperature too low (both of which are usually from overcirculation), or if there's too much CO2 to allow for an FeS film to form. In cases where there is some H2S and a lot of CO2 then its very difficult to keep the rich side clean and rich filtration is needed to protect the lean/rich exchanger.
@@adityabansod2941 The answer to your question will depend greatly on the ratio of CO2:H2S in the rich amine. Although you may have slipped a significant amount of CO2 through the absorber, what you ultimately need to know is how much did you remove, along with how much H2S was removed. If you are operating a single-absorber system, you can determine this by looking at the composition of the acid gas. In our experience acid gas with over 50% CO2 will have fouling of the lean/rich exchanger.
To form pyrrhotite, I would need high temperature and H2S. If I go to low lean loadings, wouldn't that cause me to reduce my h2s content and be less likely to form pyrrohotite in my reboiler?
Dear Sir, can you give us the minimum value of lean amine loading, that we can monitor lean amine loading higher that can form a Pyrrhotite film layer ?? how much [H2S] in lean amine is enough. ?
In any plant with H2S: you strip the amine down to a low enough loading such that the H2S concentration in the treated gas is satisfactory. In most cases this is 4ppmv. If you have less than this entering the absorber with the feed gas, then the H2S lean loading won't really matter.
Ben Spooner is a great personal with lot of hands on experience and happy to share the knowledge to the resolution permanently. This makes him entirely different. Nice video. Hope in future also will be there opportunity to work again soon.
Thanks for the video, really useful. I had a question. Is there any evidence of increase likelihood of amine SCC on the lean amine circuits when you operate at low amine loading?
Obviously the regeneration rate will be a compromise between the cost of energy use, the downtime caused by exchanger corrosion, and the OPEX for lean amine filter changeouts. Not a straightforward number.
correct. See our earlier video on "how to set steam to the reboiler" for more details!
Excellent video!! Would love to hear the rest of your thoughts on corrosion, despite sufficiently low lean loading....
Thank you for the video. I have a question for rich amine corrosion. If rich amine temperature is increased up to 85~90degC , there is corrosion in rich stream especially high pressure process even if rich loading is maintained 0.4~0.45. I know it is affected by amount of H2S flashed. What is a corrosion mechanism? is it similar to form the mackinawite ? If rich loading is enough, the pyrite is already formed.
hi there, as long as the rich loading is composed mostly of H2S (not CO2), and kept below 0.5 mol/mol (or so) there should not be any problems even if the amine is reduced from a high pressure to a low pressure, like across an absorber level control valve for example. The temperature is a concern however, in a typical carbon steel absorber we recommend 85C as the maximum "bulge" temperature to prevent corrosion of the absorber itself. Usually, the rich amine stream is slightly cooler than the bulge temperature - use a simulator to be sure, if you don't have TI's throughout the absorber - so you are putting yourself at risk by operating with 85-90C absorbers. If you have a completely stainless steel absorber, that's different and we routinely see bulge temperatures upwards of 100C.
@@benspooner8690 Thank you!
Thanks for the video, I had a question that is related to the lean/rich exchanger fouling video you did earlier. In this video you state that the high temp - high H2S conditions of the rich amine are good conditions to form the protective iron sulphide layer (pyrite), yet in the previous video, the rich side of the lean/rich exchanger is fouled and the lean side is clean. Why is this the case, it seems to be contradicting with what you say in this video?
Jared, if the rich amine conditions properly form a protective film (pyrrhotite), then you won't have fouling of the rich side of a lean/rich exchanger. The problems are when the conditions are NOT correct for the film formation. This can happen if the rich amine H2S loading is too low, temperature too low (both of which are usually from overcirculation), or if there's too much CO2 to allow for an FeS film to form. In cases where there is some H2S and a lot of CO2 then its very difficult to keep the rich side clean and rich filtration is needed to protect the lean/rich exchanger.
@@adityabansod2941 The answer to your question will depend greatly on the ratio of CO2:H2S in the rich amine. Although you may have slipped a significant amount of CO2 through the absorber, what you ultimately need to know is how much did you remove, along with how much H2S was removed. If you are operating a single-absorber system, you can determine this by looking at the composition of the acid gas. In our experience acid gas with over 50% CO2 will have fouling of the lean/rich exchanger.
To form pyrrhotite, I would need high temperature and H2S. If I go to low lean loadings, wouldn't that cause me to reduce my h2s content and be less likely to form pyrrohotite in my reboiler?
Dear Sir, can you give us the minimum value of lean amine loading, that we can monitor lean amine loading higher that can form a Pyrrhotite film layer ?? how much [H2S] in lean amine is enough. ?
How about for low h2s to Co2 ratio feed? Do you still recommend to strip all the h2s ?
In any plant with H2S: you strip the amine down to a low enough loading such that the H2S concentration in the treated gas is satisfactory. In most cases this is 4ppmv. If you have less than this entering the absorber with the feed gas, then the H2S lean loading won't really matter.