Control of Volatile Organic Compounds Emissions from Manufacturing

sources to the flare header were assumed to be 70 feet in length,8
while the length of pipelines to the flare was' based on the horizontal
distance required to provide a tolerable and safe radiation level for
conti nuous worki ng (440 ~tulhr-ft2, incl udi ng solar radi ation) .5
Piping and ducting were selected and costed as outlined in Section E.6.
E.2.2 Flare Cost Estimation Procedure. Flare purchase costs
were based on costs for diameters from 2 to 24 inches and heights from
20 to 200 feet provided by National Air Oil Burner, Inc., (NAO) during
November 1982 and presented in Table E-2.5 A cost was also provided
for one additional case of 60 inch diameter and 40 feet height.7
These costs are October 1982 prices of self-supporting flares without
ladders and platforms for heights of 40 feet and less and of guyed
flares with ladders and platforms for heights of 50 feet and greater.
Flare purchase costs were estimated for the various regulatory alternatives
by either choosing the value provided for the required height and
diameter or using two correlations developed from the NAO data for
purchase cost as a function of height and diameter. (One correlation
for heights of 40 feet and less, i.e., self-supporting flares and one
for heights of 50 feet and greater, i.e., guyed flares.) Purchase
costs of large diameter, 40-ft. high flares were approximated using a
curve developed from the NAO data (see Figure E-1). Purchase costs for
fluidic seals were approximated using a curve based on data provided by NAO~
(see Figure E-2).
A retrofit installation factor of 2.65 (see Table 5-2) was used to
estimate installed flare costs. Instal led costs were put on a June
1980 basis using the following Chemical Engineering Plant Cost Indices:
the overall index for flares; the pipes, valves, and fittings index for
pi ping; and the fabricated equipment index for duct ing. Annualized
costs were calculated using the factors presented in Table 5-3. The
flare cost estimation procedure is presented in Table E-3.
E.3 THERMAL INCINERATOR DESIGN AND COST ESTIMATION PROCEDURE
Thermal incinerator designs for costing purposes were based on
heat and mass balances for combustion of the waste gas and any requi red