Control of Volatile Organic Compounds Emissions from Manufacturing

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reductions from uncontrolled to RACT levels and the instal led capital
costs and annualized costs of achieving RACT for the three polymers.
The specific assumptions and breakdowns of capital and annual costs and
recovery credits, where appropriate, are given for each model plant in
the following sections. ,
Three cost analyses were performed for each polymer. These analyses
were made in order to reflect various control costs and emission
reductions associated with applyi ng RACT at plants that have di f ferent
existing 1 evels of control. The actual costs and emission reductions
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will depend upon the actual exi sting control level, stream characteristics
potential stream combination, and potential utilization of existing
control devi ces.
The first cost estimate is based on combining a1 1 continuous
streams that were judged to be reasonable to contro'l and delivering the8
combined stream to a single control device. Since the reduced cost of '
piping will generally not offset the increased cost of multiple control1
equi pment units, the use of a single control device for a plant is
usually the lower cost option open to a plant.
The second cost estimate is based on combining a1 1 continuous
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streams from one type of process section in a plant and delivering the '
combined stream to a single control device. This analysis reflects,
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for example, a potential situation in which a plant may be control ling
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all other emissions except those from product finishing and in order to
control product finishing emissions a new control device is required.
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The third cost estimate is, in a sense, a subset of the second
cost estimate where a plant may be controlling, for example, product
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finishing emissions from some of the lines. This estimate reflects a
'"orst case'' scenario in which a new control device is required to
control the emissions from a single process section (e.g., product
finishing) in a single process line.
5.2.1 Polypropylene (PP)
The first cost estimate was developed for 98 percent VOC destruction
by both thermal incinerators and flare control of the combined continuous
emission streams from the liquid-phase polypropylene process. The cost
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analysis is based on a fluidized bed dryer with emissions of 0.6 kg
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VOC/1000 kg of product. (Some other dryers are potentially larger
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