Control of Volatile Organic Compounds Emissions from Manufacturing

Table F-2 summarizes these costs for each of the two polymers. ThL annual
costs were adjusted as follows:
o Capital-related costs, C1,
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l
were adjusted using the equation
I
(~^)0*~
where: VI = total initial volnme of flow from model process
section and
V, = adjusted flow rate.
o Operating-related costs, Cp, were adjusted using the equa!tion
Capital-related costs included capital recovery, maintenance,'
taxes, insurance and administration charges. operati ng-related cdsts
included utilities (e.g., natural gas, steam, electricity). operating
labor was assumed to be constant.
~
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I1 I 1 I
Fourth. As flow rates vary, the size of the control device rdqui red
will also vary. No matter how small the flow, however, there are' 1
certain minimum size control devices avail able; thus, control device
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costs do not approach zero as flows become very small. In addition,
1
some utility requirements, such as natural gas purge rates, may be
constant, or even increase as flow rates become increasi ngly smal ier.
Finally, a different control device design may be more cost effective
as flow rates change. For example, as flow rates approach 1.46 sCfm
(70°F), a change in flare design was assumed to occur where a flahe
with a fluidic seal was used for flows less than 1.46 scfm. ~ablkF-3
summarizes the basic minimum costs associated with the various cothrol
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devices at flow rates that affect design criteria.
Fifth. Using the above information and procedures, the following
basic equation was solved for Vx for each process section:
whe
\ 11 and $3,000/~g
re: C; = the difference between the capital-related costs of
the control device control ling V1 and the capital -related
costs of the control device controlling V2.
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