Workshop JJ Beyond the Basics: Air Pollution Control Innovative - - PDF document

Workshop JJ

Beyond the Basics: Air Pollution Control … Innovative Control Technologies for VOC & Particulate Control — Flameless Oxidation, BioOxidation, Semi-Dry Scrubbing

Wednesday, March 28, 2018 11:15 a.m. to 12:30 p.m.

Biographical Information

Arnie T. Beringer, Owner & Managing Partner CEECO Equipment, Inc , Cincinnati, OH 513-709-8444 Fax: 513-672-0045 aberinger@ceecoequipment.com WWW.CEECOEQUIPMENT.COM Arnie began his career as an intern for the Ohio EPA (RAPCA) while he was attending the University of Dayton pursuing a Degree in Environmental Engineering. After spending an additional year with Ohio EPA after graduation, Arnie worked as an environmental engineer for Navistar for approximately 3 years in both their Springfield and Columbus Operations. After Navistar, Arnie took the environmental manager position at Sun Chemical at their pigment plant operation in Cincinnati. For the next 16 years he had various plant and regional EHS management positions and last served as the Corporate EHS Compliance Assurance Manager for the North American operations for Sun Chemical. In May of 2011 he left Sun Chemical to take over the family business, CEECO Equipment, as a manufacturer’s sales representative specializing in air pollution control and process equipment solutions. Arnie is a longtime member of the Air & Waste Management Association where he has served as the President of the Southwest Ohio Chapter on 3 separate occasions including currently. Nathan D. Hess, BioOxidation Product Manager Process Combustion Corp., 5460 Horning Rd., Pittsburgh, PA 15236 Direct: (412) 714-0069 Cell: (412) 737-7134 Fax: 412-650-5569 nhess@pcc-group.com Nathan is the Product Manager of Biological Oxidation Systems at Process Combustion Corporation (PCC). Starting as an Applications Engineer, Nathan helped acquire, develop, and commercialize the BioOxidation technology at PCC. He is involved in every phase of BioOxidation projects and is responsible for the process design and start-up of 3 full-scale systems and one pilot-scale system focused toward in-house data generation. He is continually working to advance BioOxidation solutions in a variety

• f industries, as well as expand the technology capabilities through Research &
• Development. Nathan holds a bachelor’s in Chemical Engineering from the University of

Delaware.

Biographical Information

Ron Hawks – QSEM Solutions, Inc. (A Trinity Consultants Company) rhawks@qsemsolutions.com 919-848-4003

• Mr. Hawks is expert in the evaluation, operation, and maintenance of air control

systems including capture hooding, ducting systems, scrubbers, fabric filters, electrostatic precipitators, and afterburners. He has conducted numerous internal inspections of equipment and consults regularly on system performance with industrial clients across the US. His intense knowledge of the processes within steel, coke, lime, chemical, and cement facilities, among others facilitates insight into the interaction between the processes and collection systems. His process, mechanical and collection system understanding often provides a clear path to mitigate air compliance issues driven by these complex interactions.

• Mr. Hawks has completed several control equipment evaluations and upgrades at

integrated steel mills and mini-mills, coke batteries, cement facilities, and other industries to achieve compliance with their air requirements. His experience includes thermal systems such as afterburners, RTO’s, Cement kilns, Lime kilns, abatement systems, industrial process evaluations, and other air pollution control systems.

• Mr. Hawks holds an M.M.E. in Mechanical Engineering, a B.S. in Chemistry, and a B.S.

in Aerospace Engineering, and has authored many papers on these subjects through the A&WMA and IEEE, among others. Mr. Hawks is the Process Engineering Manager and a Principle at QSEM Solutions, A Trinity Consultants Company. Michael Foggia, Business Development/Marketing Manager Process Combustion Corp., 5460 Horning Rd., Pittsburgh, PA 15236 Cell: (503)799-2372 Fax: 412-650-5569 mfoggia@pcc-group.com Michael is the National Business Development/Marketing Manager at Process Combustion Corporation (PCC). Michael has a Chemical Engineering Background – 25 years in the manufacturing sector providing proprietary chemicals and technologies to the electronics industry. 12 years in the air pollution control market providing compliance-based technologies to industry and municipalities.

• JJ. Beyond the Basics: Air Pollution Control …

Innovative Control Technologies for VOC & Particulate Control -- Flameless Oxidation, BioOxidation, Semi-Dry Scrubbing

Arnie T. Beringer – CEECO EQUIPMENT, Inc aberinger@ceecoequipment.com 513-709-8444 Ron Hawks – QSEM Solutions, Inc. (A Trinity Consultants Company) rhawks@qsemsolutions.com 919-848-4003 Michael Foggia – PCC mfoggia@pcc-group.com (503)799-2372 Nathan Hess - PCC nhess@pcc-group.com 412-655-0995

1

Air Pollution Control Technologies

• Particulate Matter (PM)

– Dust Collectors – Scrubbers – Electro Static Precipitators (ESP, WESP)

• Acid Gases, NOx, SOx

– Scrubbers/Semi-Dry Scrubbers – Dry Sorbent Injection (DSI) – SNCR, SCR

2

Air Pollution Control Technologies

• Volatile Organic Compounds (VOC)

– Scrubbers (Not very common) – Thermal Oxidation (Recup) (Incinerator) – Regenerative Thermal Oxidizer (RTO) – Catalytic Thermal Oxidizer (CTO) – Carbon Adsorption – Bio Oxidation – VOC Concentrator

3

Session JJ – Process Design Principles for Venturi Scrubbing

Columbus, OH – July 20, 2017

• Mr. Ronald Hawks, Process Manager/

Senior Managing Consultant

Agenda

˃ Process Design Methodology for Wet

Scrubbers

 Characterize Uncontrolled Particle Emissions  Define Required Control Efficiency (% mass

basis)

 Develop Design Considerations  Determine Plant Constraints

Scrubber Technology

˃ Scrubber technology has not significantly changed

since 1980’s-

 Particle capture  Droplet removal

˃ Methods of achieving the above have changed-

 Better water introduction  Better demister technology

˃ System design used by OEM’s have not changed

significantly

˃ Difficult to sell new concepts-

 Not proven in key industries  Higher installed cost  No one else is using the new concepts

Innovative Scrubber Advances

˃ Air/atomized and high pressure systems

to produce small droplets

˃ Ionized charging of water

droplet/particles to enhance capture

˃ Condensation to produce small aerosols

(nucleation Around particles)

Configuration of a Venturi Scrubber

Schematic Diagram of a Venturi Scrubber

Process Design Methodology for Wet Scrubbers

˃ Characterize Uncontrolled Particle

Emissions

˃ Define Required Control Efficiency (%

mass basis)

˃ Develop Design Considerations ˃ Determine Plant Constraints

Characterization of Uncontrolled Emissions

˃ Particle size distribution (um) ˃ Gas flow volume (wscfm) ˃ Gas temperature (0F) ˃ Gas moisture (%) ˃ Particulate (lb./hr.) mass emission rate

Expected PM Control Required

˃ Mass (lb./hr.) ˃ Concentrations basis (gr./aCF)

Design Considerations

˃ Particle capture mechanism

 Droplet size (um)  Static pressure (in/wg)  Liquid gas ratio (L/G)

˃ Water droplet separation

 Mesh pad  Chevrons  Cyclonic separation

Design Considerations (cont.)

˃ Water Management

 Once thru  Recirculation

˃ Sludge Management

 Blowdown to POTW  Dewatering

Design Considerations (cont.)

˃ Management of Sludge

 Inert  Hazardous

Particle Capture

˃ The smaller the water droplet, the higher

the capture of submicron aerosols.

˃ Droplets can be created by-

 Shearing of sheet water (i.e. overflow weir)  Preformed spray nozzles (hydraulic pressure)  Air atomized nozzles

Calculation of Scrubber Efficiency

˃ Johnstone equation ˃ Infinite throat model ˃ Cut power method ˃ Contact power theory ˃ Pressure drop

Particle Interception by Droplet

Removal Efficiency

0.00 10.00 20.00 30.00 40.00 50.00 60.00 70.00 80.00 90.00 100.00 120 150 300 450 750 1000 1500 2000 3000

%

water droplet diameter um

10um 5um

Pressure Drop

˃ ∆p=4X10-5(Vgt)2(L/G)

˃ ∆p=in H2O ˃ Vgt=throat velocity (ft./sec.) ˃ L/G=liquid to gas ratio (gal/1000 acfm)

Saturated Gas Moisture

˃ % H2O at Saturation Dependent on Absolute

Pressure in the Scrubber (Pbar-Ps) at a given Temperature

˃ % H2O at Saturation also Dependent on Gas

Composition (i.e. air vs. combustion gases)

˃ Why important?

 Water balance.  Gas saturated volume  Velocity thru demister

˃ Change in ambient barometer pressure

influences scrubber quenched gas moisture content

Intangibles for Scrubber Operation

˃ Water Droplet Size Distribution ˃ Water Droplet Spatial Distribution in the

Scrubber Throat (eliminate donut holes)

˃ Spray Nozzle Orientation During nozzle

Installation

˃ Pre-Saturation of Gas before Scrubber

Throat

˃ Sub-micron Particle Generation from

Quench Sprays

Water Droplet Carryover

˃ Failure to remove water droplets after

particle capture is the most significant impact on performance.

˃ Water droplets contain both suspended and

dissolved solids which evaporate before the Method 5 filter (248 +/- 250F) and particles are measured as filterable particulate.

˃ Impact of droplets can be determined by

comparing the measured (lb./ dry gas) to theoretical at the gas temperature and absolute pressure.

Water Droplet Carryover

˃ The lower the allowed mass emission rate, the

more significant droplet carry over becomes.

˃ A completely dry demister outlet cannot be

achieved without fouling and eventual failure.

˃ Build-up of dissolved solids in recirculated

water can result in visible plumes (NaCl, KCl, NH4Cl2 solids) which form submicron aerosols when droplets evaporate in the atmosphere.

System Hydraulic Balance Methodology

˃ Inlet gas moisture (vapor) phase ˃ Evaporation in quench section to achieve saturation

(a function of absolute pressure and temperature), an adiabatic process

˃ Condensation of water vapor due to increase in

under pressure (function of absolute pressure)

˃ Enthalpy of make-up water is usually small ˃ Enthalpy of blow-down water streams can be

insignificant

˃ Net gain or loss of water vapor at each point in the

process impacts performance

˃ Water of hydration and free water in sludge's must

be included in the balance

Heat Balance

˃ Inlet enthalpy of dry gases, water vapor,

solids must estimated

˃ Enthalpy of gases and solids at each

intermediate point in the gas stream must be calculated with changes in pressure

˃ Enthalpy of make-up streams should be

included

˃ Enthalpy of blow-down streams (liquid

and solids) should be included

Heat Balance (cont.)

˃ Final stack temperature calculated and

gas stream moisture content

˃ Inlet/outlet enthalpy must balance to

estimate final gas temperature and moisture content

˃ Iterative process using goal seek or solver

in excel between mass and heat

Semi-Dry Gas Scrubbing

Ronald Hawks, Process Manager/ Senior Managing Consultant

Components of a Dry Injection System

Components of a Spray Dryer Absorber System

Basic Principles

˃ Slurry is produced and sprayed into hot

gas stream

˃ Acid gases are absorbed into water

droplets as it evaporates

˃ An aqueous solution is produced

Basic Principles (cont..)

˃ Acid in solution reacts with base in

solution in suspension forming salt

˃ Dry salt with unreacted sorbent captured

• n a filter surface

Process Design

˃ Determine source inlet gas characteristics

(temperature, gas volume, acid gas concentration, etc.)

˃ Determine the required acid removal (%) ˃ Estimate the required sorbent injection rate

to achieve the acid gas removal (i.e. lb./lb. acid) on Ca/S molar ratio

˃ Calculate the quenched gas temperature and

moisture content

Process Design (cont..)

˃ Calculate the relative humidity of gases

passing through the filter

˃ Calculate the concentration of un-reacted

sorbent in dust

Operational Issues

˃ The approach of the quenched gas to

moisture saturation (dew point) increases acid gas removal (i.e., 150 F above saturation optimal)

˃ Condensation of water on interior

surfaces of ducts and filter walls results in fouling and corrosion unless well insulated

Operational Issues (cont.)

˃ Variation in flue gas temperature due to

boiler load, excess air and swing load demand, can result in poor performance and/or fabric fouling

˃ Design must include review of past and

expected boiler operation and gas stream conditions

Overall System SO2 Removal Efficiency

39

THE ADVANTAGES OF FLAMELESS THERMAL OXIDATION

Michael Foggia Business Development – Marketing Manager Process Combustion Corporation mfoggia@pcc-group.com 503-799-2372 27 Annual Business and Industries Sustainability and EH&S Symposium March 27 - 28, 2018 Duke Energy Center – Cincinnati, Ohio

40

Process Combustion Corporation Flameless Thermal Oxidation Process Combustion Corporation Flameless Thermal Oxidation

41

The reason why a flame is not generated in the media bed is because the gas mixture is kept below the lower flammability limit based

• n

the percentages of each organic species present. Flameless oxidation is a thermal treatment that premixes waste gas, ambient air, and auxiliary fuel prior to passing the gaseous mixture through a preheated inert ceramic media bed. Through the transfer of heat from the media to the gaseous mixture the organic compounds in the gas are

• xidized to innocuous byproducts, i.e., carbon

dioxide (CO2) and water vapor (H2O) while also releasing heat into the ceramic media bed.

What is Flameless Oxidation?

Waste gas streams experience multiple seconds of residence time at high temperatures leading to measured destruction removal efficiencies that exceed 99.9999%. Premixing all of the gases prior to treatment eliminates localized high temperatures which leads to thermal NOx as low as 1 ppmv.

42

FLAMELESS THERMAL OXIDIZER (FTO)

Functional Criteria

• A refractory lined vessel filled with ceramic

media

• Bed is preheated to initiate oxidation reactions
• Premix Waste Gas, Ambient Air, and Natural

Gas - “Feed Forward Design”

• Gas mixture below flammable range (Below

LEL)

• Oxidizing; Not Combusting
• Maximum Temperature 1800-1900°F

43

Design Benefits: High DRE……… 99.9999% Low Thermal NOx….. < 1 ppmv Low Temperatures Throughout Easy Control: Constant Volume Flow & Enthalpy (Heat)

FLAMELESS THERMAL OXIDIZER (FTO)

44

• Premixing of waste

gas, natural gas, and

• xidizing air
• Bed operating

temperature ~1800°F (1500 kJ/Nm³)

• Excess oxygen level of

~12%

• Multiple seconds of

residence time at high temperatures

How do we achieve a DRE of 99.9999%?

3 T’s of Destruction: Time, Turbulence (mixing), Temperature

Residence Time (s)

45

How do we achieve NOX emissions < 1 ppm?

Yakov Zel’dovich

Determined the correlation between temperature and NOx formation in a combustion system. Temperatures >2300F cause an exponential growth rate in NOx generation.

1800oF

46

Comparative NOx Performance

The PCC FTO achieves 50x less NOx than the Industry Standard Burner!

47

DRE NOx

High Low High Low Bio‐Oxidation Flare Thermal Oxidizer RTO FTO:  99.9999% DRE  <1ppm NOx

Competing Control Technologies NOx v.s. DRE

Indication of an underserved market

48

Where is the FTO Technology best used?

Project Parameter Regenerative Thermal Oxidizer (RTO) Catalytic Oxidizer (CO) Thermal Oxidizer (TO) Carbon Adsorption Technology Bio Oxidizer High Concentration X X Low Concentration X X X X X X Halogenated Service – Cl, Fl, Br X X X Sulfur, Mercaptans, thiols, etc. X X X X DRE 99.99% + X X Continuous Process X X Batch Process X X NOx < 1 ppmv X X X

49

Proactive Control to Manage Change

FE FIT AE AIT

LEL; BTU

TO FTO

FTO is a Smart “Feed-Forward” Reactor

• No More High/Low Temp Trips….
• No More Nuisance Shutdowns….

Great for Sold Out Products! Maximum Utilization of Production Time!

Vent Source 3 Vent Source 4 Vent Source 1 Vent Source 2

50

51

FTO APPLICATION FITS

Best fits are high end customers requiring very low NOx, very high DRE, and high reliability such as pharmaceutical & specialty chemical companies. Also best with clean waste streams with reasonable

• rganic heating value.

52

Example FTO Installation

System Burner (Start-up Only) Dip Tube

53

VOC’s

Chemical Reactions In Air

NO2 HNO3 O2 N2O NO Accumulation Acid Rain Combustion Activities O3 (Ozone) Smog

54

55

Performance Beyond Compliance

FTO Permit Benefits:

1) Generate emission credits that can be banked or sold 2) Allow for plant expansions without modifying an existing air permit

In a typical ozone Nonattainment New Source Review project, one requirement is to offset the project emissions of the ozone precursor (NOx or VOCs) with emission reduction credits (ERCs) obtained from a source within the nonattainment area.

ERCs in the Gulf Coast can cost up to $400,000 per ton!

Lowering stationary source emissions through the use of a Flameless Oxidizer can prevent having to purchase ERCs and may in fact generate ERCs that can be used to expand a plant or sold.

56

Flameless Oxidation

Values Feature Benefit Low NOX

Low Temperature Premixed Oxidation <1 ppmv NOx

High DRE

Premixed Oxidation; 3-4 seconds RT; 99.9999% DRE

Up-Time

Stable/Resilient Oxidation Environment; Feed forward control; No Moving Parts; No thermal cycling of media bed (Long ceramic Life) > 99% Uptime

Easy Permitting

Eliminate requirement for CEMS (High Performance Oxidizer Reactor) Less time to permit

ROI

Lower emissions; Emission Trading opportunity; Ease of site expansion Lower Permitting Costs, Emission Credits, Added Reliability (More Production)

Operational Flexibility Multiple control set points; 100% Waste gas

turndown; Accept varying waste compositions “Ready-Idle” mode to limit fuel use & Stable Operation

PCC FTO Your Environmental Competitive Advantage

57

THANK YOU

PCC BioOxidation

Outline

• BioOx Basics
• Technology Development: BioOxidation vs.

Traditional Biofiltration

• Technology Comparison: BioOxidation vs. RTO
• Applications
• 1. Wood Products Process
• 2. Asphalt Process
• PCC BioOx Research and Development

BioOxidation System Asan, South Korea

Why add BioOxidation?

 PCC wanted the ability to offer a “non‐thermal” solution where appropriate  Better alternative to RTO’s in many applications (high flow, low concentration)  Dual‐BioPhase Technology is new and innovative  “Green” Technology  Does not consume Natural Gas  Does not generate NOx SOx CO  Produces ~90% less CO2 vs. Thermal Oxidation  Operates at ambient temperature and low pressure

Biological Oxidation (Biofiltration):

• Process whereby contaminants transfer from air phase to biofilm.
• Biodegraded by microorganisms.
• Biofilm is the primary element of the Bio‐Oxidizer

involved in the destruction of the contaminants.

• As Biofilm continually grows, it must slough off to

maintain a healthy microbial colony.

Pollutant + Bacteria + Oxygen + Nutrients  CO2 + H2O + More Bacteria

BioOx Basics

“Microorganism” refers to a wide variety of single cell,

live bacteria. Given sufficient time and quantities, bacteria can biodegrade nearly anything.

Microbes

a.k.a Bacteria or Bugs

FREEZE DRIED MICROORGANISMS NUTRIENT ADDITIVE

FAQ>>> “What happens if the Bugs get out of the bio‐oxidizer unit?”

Nothing…………….

Bacteria is Everywhere in Nature

• We utilize naturally occurring bacteria.
• We create an environment which allows them to work in an

enhanced and significantly more efficient manner than typically found in nature.

a.k.a Bacteria or Bugs

Microbes

Evaluation Category Organic Media Dual-BioPhase™ Synthetic Media

Microorganisms and Nutrients are Restrained within Media Yes No Media Replacement is Required to Replenish Nutrients Yes No Media needs Continually Fluffed to Obtain Porosity Yes No Biomass Growth Causes Media Settling Yes No Continually Increasing ΔP Yes No Maintaining Optimal Water Content is Crucial Yes No

Media Height Limited to Maintaining Proper Moisture Content

Yes No Capacity for Contaminants - ppmv <50 <5,000 Limited Capacity to Neutralize Acids Yes No

Biological Media Development

X X X X 

X



Biofilm – Biomass - Slough off

Open Biofilter System

Humidifier Compost Filter Bed (about 1 meter in depth) Gravel Ground Foul Air

Technology Development: BioOxidation vs. Biofilter

OLD TECH

 Limited Bed Depth  Media Replacement Necessary  Poor Removal Efficiency due to Dry-out and Channeling

Bed Compaction Channeling Channeling

Early Bio‐Filter Designs

Removing Failed Media Old Media Old Style Biofilter Overall footprint 100’ x 170’

X

PCC BioOxidizer System

Contaminant

Ambient Air Water Soluble Pollutants are Treated in the Liquid Phase Less Soluble Pollutants are Treated in the Gas Phase Nutrient Enriched Feed Recirculating Loop to Aeration Mixer

PCC NEW TECH

 Mass Transfer to Liquid Maximized  Biological Oxidation in 1) Liquid and 2) Gas Phase  Footprint Minimized

BIO BIO

ABSORBER

Traditional Biofilter

Bio-Oxidizer Footprint

Technology

BioOxidation vs. Biofilter

Category Typical Biofilter Dual-BioPhase™ Bio-Oxidizer Footprint Very Large ~6-8 Times Smaller Media Replacement Periodically possible Not Required Fouling/Plugging Potential Plugging Anti Fouling Design Nutrients Manual Addition, bulk Metered delivery system Water Blow Down Potential Black Water Treated Water Start Up Inoculation Waste Water Bacteria Selected per Contaminant Start Up Food Source Molasses Contaminant – Waste Stream Pressure Drop Potential Gradual Increase Stable VOC Removal Limited Potential >95% DRE

BioOxidation System Advantages

Technology Comparison: PCC BioOx vs. RTO

Category RTO Dual-BioPhase™ Bio-Oxidizer Natural Gas Usage Yes $$$ None required Operating Temp 1500F – 1600F Ambient 60F – 150F (wet bulb) Fire Hazard Potential No – Humid, Wet System Maintenance Valve wear & Tear No Major Moving Parts Fouling/Plugging Potential Plugging Anti Fouling Design Media Change Out Probable No CO, NOx Emission Yes No SOx Emission Potential No CO2 Emission Yes ~90% Less Post Treatment Potential No

Technology Comparison: PCC BioOx vs. RTO

BURNING YOUR PROFITS ?

Parameter BIO RTO1 Electric Usage (kW) 459.0 352.8 Electric Cost2 $241,258 (¥1.6 MM) $185,411 (¥1.2 MM) Nutrient Cost $20,000 (¥130,000)

• Natural Gas Cost3
• $756,232

(¥5.0 MM)

• Min. Total Operating Cost4

$261,258 (¥1.74 MM) $941,643 (¥6.3 MM) Maintenance Cost Less More CO2 Generation (tpy) 690 19,386

Engineered Wood Products Application: Flow rate: 215,000 acfm; Loading: 165 lb/hr VOC

PCC BioOx and RTO Operating Cost Comparison

(365,300 m3/hr) (75 kg/hr)

$680,000 (¥ 4.5 MM) Less Operating Cost 96.4 % Less CO2 emitted

First thermophilic gas‐phase BioOxidizer in the world

WOOD PRODUCTS

PB = Particle Board PW = Plywood OSB = Oriented Strand Board MDF = Medium Density Fiber

PB PW OSB MDF

Width: 33 ft 10 m Height: 90 ft 27 m 330,000 acfm 140 °F

Mist Eliminator Bed

Gas Phase Biological Media Bed

Absorption Media Bed

Liquid Irrigation

(6,500 gpm; 1,476 m3/hr)

Liquid BioOxidation Section

Aerator Manifold and Liquid BioMedia

Biofilm

DRE Hydrogen Sulfide 98.7% Methyl Mercaptan 98.7% Acetaldehyde 71.7% Propionaldehyde 19.4% Isovaleraldehyde 40.0%

Asphalt Plant Emission Control

Height: 52ft 15.7m Diameter: 12ft 3.7m

FULL SCALE TESTING

HEATED PROBE STACK WALL ISOLATION VALVES CONDENSER CONDENSER MIDGET IMPINGER

(WITH DISTILLED WATER)

GAS DRYER DRY GAS METER VACUUM PUMP ROTAMETER

COOLING WATER LOOP

ADSORBEN T TUBE Send impinger water (methanol and formaldehyde capture) and carbon tube (pinene capture) to lab for quantitative analysis

Heated probe Glassware box – condensers, liquid impinger, and carbon adsorbent tube Ice bucket for condenser cooling loop Console – vacuum pump, flow control, and gas meter Sampling train is connected to console with heated umbilical cord

10 20 30 40 50

FID 1

10 20 30 40 50

FID 2

10 20 30 40 50

FID 3

10 20 30 40 50

FID 4

10 20 30 40 50

FID 5

10 20 30 40 50

FID 6

10 20 30 40 50

FID 7

10 20 30 40 50

FID 8

10 20 30 40 50

FID 9

AVG 38.75 SD 3.52 RSD 9.08% Time 31 min AVG 39.18 SD 1.10 RSD 2.82% Time 28 min AVG 45.55 SD 0.74 RSD 1.64% Time 28 min AVG 47.86 SD 0.78 RSD 1.63% Time 28 min AVG 42.34 SD 0.77 RSD 1.82% Time 28 min AVG 47.05 SD 0.86 RSD 1.82% Time 14 min AVG 34.47 SD 0.67 RSD 1.94% Time 28 min AVG 32.70 SD 0.89 RSD 2.72% Time 27 min AVG 30.81 SD 0.78 RSD 2.53% Time 26 min

EWP Outlet Gas Sampling Data – March 13, 2017

y = 1.2587x + 0.1142 R² = 0.9995 y = 1.418x R² = 1 0.0 5.0 10.0 15.0 20.0 25.0 0.0 5.0 10.0 15.0 20.0

Volume (L) Time (min)

S3

Stready State Initial Linear (Stready State) Linear (Initial) y = 1.2424x ‐ 0.7249 R² = 0.9997 y = 0.758x R² = 1 0.0 5.0 10.0 15.0 20.0 25.0 0.0 5.0 10.0 15.0 20.0

Volume (L) Time (min)

S2

Stready State Initial Linear (Stready State) Linear (Initial) y = 1.2063x ‐ 0.926 R² = 0.9979 y = 0.722x R² = 1 0.0 5.0 10.0 15.0 20.0 25.0 0.0 5.0 10.0 15.0 20.0

Volume (L) Time (min)

S1

Stready State Initial Linear (Stready State) Linear (Initial)

Location Stack Date 3/14/2017 Starting time 10:41 AM Duration (min) 17.00 Mid time 10:49 PM Notes Sample 1 Starting volume (L) 8,152.039 Sampling Rate (L/min) 1.206 Total Volume (L) 20.281 Min Sec Min Adjusted Meter Reading (L) Sample Volume (L) 0.00 8,152.039 0.000 30 0.50 8,152.400 0.361 1 1.00 8,152.600 0.561 1 30 1.50 8,153.000 0.961 2 2.00 8,153.812 1.773 2 30 2.50 8,154.543 2.504 3 3.00 8,155.123 3.084 Location Stack Date 3/14/2017 Starting time 2:16 PM Duration (min) 15.00 Mid time 2:23 PM Notes Sample 2 Starting volume (L) 8,172.500 Sampling Rate (L/min) 1.242 Total Volume (L) 18.450 Min Sec Min Adjusted Meter Reading (L) Sample Volume (L) 0.00 8,172.500 0.000 30 0.50 8,172.879 0.379 1 1.00 8,173.568 1.068 1 30 1.50 8,174.334 1.834 2 2.00 8,174.976 2.476 2 30 2.50 8,175.381 2.881 3 3.00 8,176.065 3.565 Location Stack Date 3/14/2017 Starting time 3:13 PM Duration (min) 13.50 Mid time 3:20 PM Notes Sample 3 Starting volume (L) 8,193.023 Sampling Rate (L/min) 1.259 Total Volume (L) 17.147 Min Sec Min Adjusted Meter Reading (L) Sample Volume (L) 0.00 8,193.023 0.000 30 0.50 8,193.732 0.709 1 1.00 8,194.440 1.417 1 30 1.50 8,195.059 2.036 2 2.00 8,195.500 2.477 2 30 2.50 8,196.248 3.225 3 3.00 8,196.982 3.959

EWP Outlet Gas Sampling Data – March 13, 2017

HAP Gas Sampling Results (11/9/16) Stack 1 Inlet 1 Stack 2 Inlet 2 Date 11/7/201 6 11/7/201 6 11/8/201 6 11/8/201 6 Total sample volume (L)1 14.995 10.639 9.843 7.928 Steady state sampling flow rate (mL/min)2 495.1 622.7 483.7 578.0 Sample quantity (gmol)3 0.4624 0.3281 0.3035 0.2445 Methanol Measured mass (μg) 0.937 64.7 0.957 36.6 Mass flow rate (lb/hr)4 0.042 3.798 0.066 2.884 Gas Concentration (ppmv)

• 0. 063

6.155 0.098 4.673 Mass DRE 98.89% 97.72% Concentration DRE 98.97% 97.89% Formaldehyde Measured mass (μg) 0.756 33.0 4.01 17.3 Mass flow rate (lb/hr) 0.034 1.937 0.275 2.884 Gas Concentration (ppmv) 0.054 3.350 0.440 2.356 Mass DRE 98.24% 79.83% Concentration DRE 98.37% 81.33%

Contaminant masses were quantitatively measured by Gas Chromatography and Spectrophotometry.

and flow rate calculation is shown in Appendix B.

‐0.98 iwc).

respectively.

EWP Outlet Gas Sampling Data – November 9, 2016

PILOT SCALE TESTING

DUAL-BIOPHASE™ R&D/PILOT PLANT

Thank You Questions?!

Level Description Hazard level Lab requirements Examples BSL‐1 Low‐risk microbes Little to no threat No containment required Nonpathogenic strain of E. coli BSL‐2 Human disease Moderate health hazard Reduce aerosol Lyme disease Pathogenic and infectious Some containment Human immunodeficiency virus (HIV) Autoclave Hepatitus A, B, C Pathogenic E. coli Staphylococcus aureus Salmonella BSL‐3 Indigenous or exotic Serious, lethal hazard Mainly government agencies Yellow fever Lab personnel under medical surveillance West Nile Evacuated airflow Tuberculosis Restricted and controlled Chikungunya High containment Venezuelan equine virus BSL‐4 Dangerous and exotic Frequently fatal Showering upon exit Ebola Decontamination of all materials Marburg virus Positive pressure suit Extremely isolated Maximum containment

*Only ~50 BSL‐4 labs in the world

Biological Safety Level

Contaminant

Biodegradabilit y

Aliphatic Hydrocarbons (Methane, Propane, Butane….) 1 Chlorinated Compounds 1 Sulfur‐containing carbon compounds (Dimethyl sulfide ) 1‐2 Nitrogen‐containing carbon compounds (Amines) 1‐3 Ethers 1‐3 Aromatic Hydrocarbons (Toluene, Phenol, Xylene, Styrene) 2‐3 Alcohols 3 Aldehydes 3 Carbonic Acids (Vinyl Acetate, Ethyl Acetate, Butyl Acetate, Isobutyl Acetate) 3 Ketones (Acetone, MEK, Methyl Isobutyl Keynote) 3 Inorganic Compounds (Ammonia, Hydrogen Sulfide) 3

CHEMICAL BIODEGRADABILITY

OPTIMAL EFFLUENT FACTORS

• Thermophilic microbes for 125o - 165oF wet bulb.
• Mesophilic microbes for 60o – 110oF wet bulb.

Condenser 1 Portable Flame Ionization Detector (FID) – immediate measure of total Hydrocarbons Water impinger (methanol and formaldehyde) Heated probe Condenser cooling loop Condenser 2 Adsorbent tube (pinene) connection spot Gas dryer to protect vacuum pump 3 way valve (to purge line)

Thank You!! Questions or Additional Information:

Arnie Beringer, Owner, CEECO Equipment, Inc. aberinger@ceecoequipment.com 513-709-8444 www.ceecoequipment.com