Fooling around with a summarization tool. Below is what it did with David
Keith's article on his air-liquid contactor (Holmes & Keith 2012).  The
first thing I notice is that the abstract from the article would be more
useful!

I am interested in thoughts on what the summarizer could have done better
on this article.

http://keith.seas.harvard.edu/papers/148.Holmes.Keith.ContactorForLargeScaleCapture.e.pdf

Additional results are available at
http://www.pagekicker.com/index.php/catalog/document-analysis-results/700000129.html

* The core simplification of this cost model is that, for a slab geometry
contactor, the shell cost is roughly independent of the depth of the
packing.
* For example, the cost of a contactor shell with a 20 × 200 m frontal area
does not change significantly as the thickness of the packing is varied from
3 to 15 m. As discussed in §2e, the CO2 mass flux into the liquid is always
proportional to the concentration of CO2 in the overlying air so that it
can be expressed as a liquid-phase mass transfer coefficient KL (with units
of velocity) times the CO2 mass density in the air [5].
* Because the flux of CO2 into a liquid hydroxide solution under conditions
relevant to AC is proportional to the mixing ratio of CO2 in the overlying
gas, the mass transfer coefficient therefore has the units of velocity.
* We find that the cost of air contacting can be of the order of $60 per
tonne CO2 with a contactor design that results in a capture fraction of 80
per cent.
* Finally, we note that the fourfold discrepancy between our estimate of
contactor cost and that in the recent APS DAC report is due to
fundamentally different design choices, insufficient optimization in the APS
design and our choice of lower-cost contactor internals.



Fred Zimmerman
Ann Arbor, Michigan, USA
"a fox, not a hedgehog" -- Isaiah Berlin

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