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Date: November 6, 2012 

Subject: National Emission Standards for Hazardous Air Pollutants (NESHAP) Beyond 

the Maximum Achievable Control Technology (MACT) Floor (‘Beyond-theFloor’) Analysis for Revised Proposed Emission Standards for New Source Coaland Oil-fired Electric Utility Steam Generating Units 

From: Nick Hutson, U.S. EPA Office of Air and Radiation 

To: Docket No. EPA-HQ-OAR-2009-0234 

Introduction 

The purpose of this memorandum is to present the data, methodology and assumptions used to 

conduct a beyond-the-floor (BTF) analysis for the emission limits that the Agency is proposing 

in the reconsideration of certain new source standards established in the final National Emission 

Standards for Hazardous Air Pollutants (NESHAP) for Coal- and Oil-fired Electric Utility Steam 

Generating Units (EGUs). This memorandum presents the estimates of the incremental pollutant 

emission reduction and cost that would be achieved by implementing a BTF option to control 

hazardous air pollutant (HAP) and HAP surrogate emissions from new and reconstructed sources 

and discusses any anticipated non-air quality health and environmental impacts and energy 

requirements. 

The MACT floor level of control for new EGUs is based on the emission control that is achieved 

in practice by the best controlled similar source for each HAP or HAP surrogate in the different 

categories or subcategories. After EPA establishes MACT floor levels, CAA section 112(d)(2) 

requires EPA to consider whether more stringent BTF standards should be established. Pursuant 

to that section of the CAA, the Agency must consider “the cost of achieving such emission 

reduction, and any non-air quality health and environmental impacts and energy requirements...” 

before it may establish a standard that is based on a BTF level of control. 

As mentioned, the new source MACT floor emission limits were set based on the performance of 

the best controlled similar source within that category or subcategory. In most of these cases, it is 

reasonable to expect that the very best performing source is achieving that level of control 

through the application of well-performing control technologies, by following a disciplined and 

routine maintenance schedule, and by operating in an efficient manner. For most of the new 

source standards addressed in the reconsideration proposal, we have not identified additional 

technologies or HAP emission reduction approaches that would achieve HAP reductions greater 

than the new source floors for the subcategories – other than multiple controls in series (e.g., 

multiple scrubbers in series or multiple particulate matter (PM) controls in series), which we 

consider to be unreasonable from a cost perspective. We are therefore proposing to adopt the 

floor level of control in all but one instance. We are proposing a BTF standard for hydrogen 

chloride (HCl) emissions from coal-fired EGUs. Details of the EPA’s BTF evaluations for the 

new source standards proposed in the reconsideration notice are provided below. 
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Beyond-the-floor analysis for PM from coal-fired EGUs 

It is commonly accepted that a baghouse fabric filter (FF) is the technology that provides the best 

level of PM emission reduction for coal-fired EGUs. Newly constructed coal-fired EGUs will be 

expected to install a baghouse FF to meet the new source NESHAP PM limit and the applicable 

New Source Performance Standard (NSPS). We have considered available options that would 

allow a new source to achieve greater emission reductions than those achieved in practice by the 

best controlled source. The EPA is aware that some EGUs have installed downstream secondary 

PM control devices to provide for incremental PM reductions beyond what is achieved by the 

primary PM control device. However, those secondary “polishing” PM control devices are most 

often installed for one of two purposes: (1) to augment the control of an underperforming or 

undersized primary control device, or (2) to allow for injection of activated carbon or other 

powdered sorbent so that the fly ash and the sorbent remain separated for eventual storage, 

disposal, or re-use. A wet ESP (WESP) may also be installed in a new coal-fired EGU (usually 

downstream of a wet-flue gas desulfurization (WFGD) scrubber). Although the primary purpose 

of the WESP would be to control emissions of condensible PM (especially sulfuric acid mist), it 

would be expected to also provide some small incremental reduction in filterable PM emissions. 

We have conducted a BTF analysis on a hypothetical new 500 MW plant burning coal with an 

ash content of approximately 10% and operating at an 85% capacity factor. The calculation 

assumed that the primary PM control device is a fabric filter with an air-to-cloth ratio of 4.0, and 

that it is designed to meet a filterable PM (fPM) emission level of 75% of the proposed emission 

limit of 0.09 lb/MWh.1

 Although a relatively small percentage of the coal ash would be expected 

to partition to the bottom ash, we assumed all of the coal ash content would exit the system as fly 

ash. 

We then calculated the BTF incremental cost effectiveness for installation of a downstream 

“polishing” secondary PM control device. In this case, we assumed the downstream FF would 

have an air-to-cloth ratio of 6.0 and that it would provide incremental fPM control to achieve an 

emission that is 50% of the proposed emission limit of 0.09 lb/MWh. In this case the polishing 

PM device would remove a much smaller amount of fPM, but at a similar (though lower) overall 

costs than the primary PM control device. The incremental cost effectiveness was calculated to 

be greater than $75,000 per ton of fPM. We do not believe that this is a reasonable cost per ton 

removal and it does not justify the installation of the downstream secondary PM control device 

and, therefore, we are not proposing a BTF fPM emission limit. 

Beyond-the-floor analysis for Hg from EGUs firing non-low rank virgin coal 

The proposed new source mercury (Hg) emission limit for EGUs firing non-low rank virgin coal 

is based on the use of the three times the representative detection level (3xRDL) approach and, 

thus, a more stringent BTF limit would be impractical due to measurement frequency issues 

described in the preamble to the proposed rule. As explained in the preamble and in the 

associated technical support memo (“Determination of Representative Detection Level (RDL) 

                                                           

1

 In petitions for reconsideration, petitioners stated that operators usually target emissions that 

are 50 – 75% of the emission limitation to provide for margin of error. 
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and 3xRDL Values for Mercury Measured Using Sorbent Trap Technologies”, which is available 

in the rulemaking docket, EPA-HQ-OAR-2009-0234), we do not have information available to 

determine at this time whether a lower Hg emission limit could be reliably measured with 

sufficient frequency to allow consistent and timely compliance. For this reason, we have 

determined that it is not reasonable to establish a BTF level of control for Hg from this 

subcategory. 

Beyond-the-floor analysis for Hg from EGUs firing low rank virgin coal2

The proposed new source Hg emission limit for EGUs firing low rank virgin coal is based on the 

performance of an existing EGU that is equipped with advanced air pollution control technology, 

including injection of brominated activated carbon upstream of a FF for the control of Hg. 

Although it is reasonable to assume that an increase in the injection rate of the brominated 

activated carbon would result in better performance and, thus, lower emissions, we do not have 

enough information to determine whether or not the increase in sorbent would result in a 

reduction in emissions that is cost-effective. 

The sorbent performance curve (i.e., the percent of Hg reduction versus sorbent injection rate – 

see Figure 1 for an illustrative example) tends to have a steep area where small increases in 

sorbent result in large increases in Hg removal. However, as the sorbent injection approaches its 

performance limitation, the curve becomes flat and large increases in sorbent are required for 

only small incremental improvements in Hg control. 

Figure 1. Example sorbent injection performance curve 

The sorbent injection curve tends to be very site specific and we have no way to know exactly 

how the sorbent injection curve for a new low rank coal-burning source would look. We believe 

                                                           

2 As stated in the preamble to the proposed rule, EPA is taking comment on whether to revise the 

Hg limit for EGUs firing low rank virgin coal based on the additional data in the record. 

0

10

20

30

40

50

60

70

80

90

100

Mercury Control,

%

Increasing Sorbent Injection ‐‐‐‐‐‐>
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that it is likely that the performance needed to achieve a BTF level of control would require a 

considerable increase in activated sorbent injection. Such a significant increase would result in 

higher levels of sorbent mixed with the fly ash, which may affect the viability of the resulting fly 

ash-sorbent mixture to be recycled for beneficial use (e.g., in concrete manufacture or in road 

construction) and, thus, its salability. Fly ash that cannot be beneficially recycled must be landfilled at considerable cost. 

A BTF analysis was performed on a hypothetical new 500 MW plant burning low rank virgin 

coal and operating at an 85% capacity factor. It was assumed that the fuel used in the EGU has 

an average Hg content of 26.2 lb/TBtu (which was the average Hg content of low rank virgin 

coal from the 2010 Utility information collection request (ICR)). Based on data from U.S. 

Department of Energy (DOE) National Energy Technology Laboratory (NETL) field tests, we 

estimate that such a facility should be able to achieve a targeted emission of 75% of the proposed 

emission limit of 0.03 lb/GWh (or 0.0225 lb/GWh, which is an approximately 92% reduction, 

coal-to-stack for the average coal) by injecting 2 lb/MMacf (pounds of sorbent per million actual 

cubic feet of flue gas) of brominated activated carbon sorbent upstream of a well-performing 

FF.3

 We have also assumed that the EGU would need to increase the sorbent injection – to 5 

lb/MMacf – to achieve a BTF emission of 50% of the proposed emission limit (or 0.015 lb/GWh, 

which is an approximately 95% reduction, coal-to-stack). 

The increase in sorbent injection needed to achieve the BTF emission may render the captured 

fly ash (or spray dryer absorber (SDA)/FF byproduct) unfit for beneficial reuse. If the fly ash 

cannot be sold (or given away in the case of SDA/FF byproduct) for beneficial reuse, then the 

operator must landfill the resulting byproduct-sorbent mixture at considerable cost. In the 

DOE/NETL study (cited earlier), this tended to increase incremental costs ($ per pound of Hg) 

by approximately three-fold for plants firing low rank coal. 

In the cost analysis for the hypothetical new plant, we calculated incremental BTF costs ranging 

from $61,000 per incremental pound of Hg (assuming no byproduct effects) to $183,500 per 

incremental pound of Hg (assuming the sorbent renders the byproducts unusable). We do not 

believe that this range of potential incremental cost effectiveness is reasonable, therefore, we are 

not proposing a BTF Hg emission limit for new units designed for and burning low rank virgin 

coal. 

Beyond-the-floor analysis for SO2 emissions from coal-fired EGUs 

The best performing source for sulfur dioxide (SO2) emissions from a coal-fired EGU is a 

circulating fluidized bed combustor (CFB) with limestone injection for SO2 control and a 

downstream circulating dry scrubber (CDS) for supplemental SO2 control. This is expected to be 

a common and well-performing control configuration for new CFB combustors. Other generation 

                                                           

3 Jones, A.P.; Hoffman, J.W.; Smith, D.N.; Feeley, J.; Murphy, J.T.; “DOE/NETL’s Phase II 

Mercury Control Technolgoy Field Testing Program: Preliminary Economic Analysis of 

Activated Carbon Injection”, Environ. Sci. Technol., 41, 1365 (2007); and Sjostrom, S.; Durham, 

M.; Bustard, C.J.; Martin, C.; “Activated Carbon Injection for Mercury Control: Overview”, 

Fuel, 89, 1320 (2010). 
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technologies (i.e., PC boilers) will be expected to install advanced FGD technology such as spray 

drier absorber (SDA) for lower sulfur coal or a wet-FGD scrubber (WFGD) for units burning 

medium-to-high sulfur coals. A unit burning high sulfur coal (approximately 4% S, e.g., coal 

mined in the Illinois basin) would need to control to greater than 98% in order to meet the 

proposed revised new source MATS SO2 limit (or nearly 99% in order to provide an operating 

margin). This level of performance is considered state-of-the-art and we believe the only 

opportunity to achieve a BTF emission level would be to install a downstream “polishing” 

scrubber. We do not believe that would be a cost effective option. 

We have conducted a BTF analysis on a hypothetical new 500 MW plant burning coal with a 

sulfur content of approximately 4% and operating at an 85% capacity factor. The calculation 

assumed that the primary FGD device is designed to meet an SO2 emission level of 75% of the 

proposed emission limit of 1.0 lb/MWh. We then calculated the BTF incremental cost 

effectiveness for installation of a downstream “polishing” secondary scrubber. We assumed the 

downstream scrubber would provide incremental SO2 control to achieve an emission that is 50% 

of the proposed emission limit of 1.0 lb/MWh. For cost assumptions, we used information in 

Table 5-4 (Illustrative Scrubber Costs (2007$) for Representative Sizes and Heat Rates under the 

Assumptions in EPA Base Case v.4.10) from Chapter 5 (Emission Control Technologies) of the 

Integrated Planning Model (IPM) v 4.10 documentation. We calculated that the incremental cost 

effectiveness would be greater than $27,000 per ton of SO2 removed. We do not believe that the 

cost of going BTF is reasonable and, therefore, we are not proposing a BTF SO2 emission limit. 

Beyond-the-floor analysis for PM from solid oil-derived fuel-fired EGUs 

 This analysis is very similar to that which was presented earlier for PM emissions from coalfired EGUs. We believe that the incremental costs would be very similar to those presented for 

coal-fired EGUs. As with the coal-fired source, such a device would add considerable costs to 

the project, and the incremental cost effectiveness (i.e., the $/ton for the incremental PM 

reduction – which was calculated at > $75,000 per ton of fPM for new coal EGUs) would not be 

reasonable. 

Beyond-the-floor analysis for SO2 from solid oil-derived fuel-fired EGUs 

The best performing source for SO2 emissions from solid oil-derived fuel-fired EGUs is a CFB 

combustor with limestone injection for SO2 control. Solid oil-derived fuel is most often fired in 

CFB boilers; and, as mentioned earlier, this limestone injection control configuration will be the 

most commonly used for CFB boilers. The proposed new source emission limit for SO2 is the 

same as for the coal-fired EGU subcategory (1.0 lb/MWh) and the same arguments present 

earlier for why we do not believe that installation of a downstream scrubber is cost effective can 

also be made here. For coal-fired EGUs, we calculated that the incremental cost effectiveness 

would be >$27,000 per ton of SO2 removed and we believe that the costs would be the same or 

very similar for solid oil-derived fuel EGUs. We do not believe that the cost of going BTF is 

reasonable, and, therefore, we are not proposing a BTF SO2 emission limit. 

Beyond-the-floor analysis for PM from continental liquid oil fuel-fired EGUs 
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The proposed new source fPM emission limit for continental liquid oil-fired EGUs is based on 

an EGU that uses an electrostatic precipitator (ESP). Distillate oil-fired facilities do not need 

add-on PM controls (their emissions are inherently low) and residual oil-fired EGUs cannot use 

FFs for PM control due to concerns about bag contamination and fire safety. Therefore ESPs are 

the best filterable PM control technology for liquid oil fuel-fired EGUs. The proposed new 

source emission limit is 0.4 lb/MWh. The performance of an ESP is based on the properties of 

the ash (particle size, particle resistivity, etc.). We do not have the necessary information to 

determine if a BTF level of performance can be obtained at liquid oil-fired EGUs and therefore, 

we are not proposing a BTF emission limit. 

Beyond-the-floor analysis for all HAP emissions from IGCC EGUs 

We have no data upon which to assess whether any other technology would provide additional 

control, in a cost effective manner, beyond the proposed new source emission limits for HAP 

emissions from new IGCC EGUs. Accordingly, we are not proposing to establish BTF emission 

limitations for these pollutants for new IGCC EGUs. 

Beyond-the-floor analysis for HCl emissions from coal-fired EGUs 

For HCl, the EPA’s revised floor analysis for coal EGUs resulted in a revised MACT floor of 

0.020 lb/MWh. We have estimated that a new coal-fired EGU would need to remove HCl in the 

range of 81.0 to 96.6 % (depending upon the initial chlorine (Cl) content of the fuel) in order to 

meet this revised MACT floor emission standard. We also note that it is reasonable to expect that 

in most, if not all, cases, advanced FGD control technology (such as a WFGD scrubber or a high 

efficiency SDA) would be required as a result of other federal requirements – specifically a 

prevention of significant deterioration (PSD) best available control technology (BACT) analysis. 

A high efficiency SDA is less costly than a WFGD, and we think it likely that some new sources 

will be able to comply with PSD/BACT requirements using that less expensive option. For this 

reason, we believe that it is reasonable to assume the minimum level of performance for HCl 

control from a new EGU will be equivalent to that of a well-performing SDA for purposes of the 

BTF analysis. We examined the level of HCl control achieved by those EGUs from the 2010 

Utility ICR database that were equipped with SDA and we determined that those EGUs achieved 

HCl control in a range of 90 to 98 percent (coal-to-stack, depending on the coal Cl content). 

In addition, because we have determined that no additional controls will be required to comply 

with a BTF level of control for HCl, we do not believe that there are any non-air quality health or 

environmental impacts or additional energy requirements associated with establishing a limit 

based on a BTF level of control. 

We therefore are proposing to set a BTF HCl emission limit for new coal-fired EGUs at 0.010 

lb/MWh. We believe that a new EGU firing lower Cl-content coal would need to achieve a 

minimum of 90 percent control to meet this proposed limit and that a new EGU firing a higher 

Cl-content coal would need to achieve a minimum of 98 percent control to meet the limit. We 

believe that this BTF emission limit is cost-effective because it does not involve additional cost 

as we expect that any new EGU will need to install at least a high efficiency SDA to comply 

with other CAA requirements. 
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We also considered a BTF emission limit by assuming installation of a WFGD scrubber, which 

generally achieves greater HCl reductions, but at somewhat greater cost, than a high efficiency 

SDA. We understand that some new coal-fired EGUs will likely be required to install this type of 

advanced FGD technology for SO2 control. However, if the EGU is not required to install a 

WFGD scrubber as a result of the PSD BACT determination for SO2, then the additional costs 

beyond those for a high efficiency SDA would be attributable only to the achievement of 

additional HCl emission reductions. For cost assumptions, we used information in Table 5-4 

(Illustrative Scrubber Costs (2007$) for Representative Sizes and Heat Rates under the 

Assumptions in EPA Base Case v.4.10) from Chapter 5 (Emission Control Technologies) of the 

Integrated Planning Model (IPM) v 4.10 documentation. We calculated the incremental cost for 

the WFGD scrubber to be $11,404 per ton of HCl removed. We do not find this to be cost 

effective and, thus, we are proposing a BTF value of 0.010 lb/MWh.