“oil lakes” monitoring and assessment report ims · 2015-01-04 · “oil lakes” monitoring...

“Oil Lakes” Monitoring and Assessment Report

Volume 2, Appendix F:

High-Temperature Thermal Desorption System Preliminary Design

Monitoring and Assessment of the Environmental Damages and Rehabilitation in the Terrestrial Environment (Cluster 3)

UNCC Claim 5000432

27 August 2003

Consortium of International Consultants (CIC) Kuwait Office

Telephone: +965 533 2723 Facsimile: +965 532 7050 Email: [email protected]

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Consortium of International Consultants I

TABLE OF CONTENTS 1 Design Rationale ............................................................................... 1

1.1 High Temperature Thermal Desorption Bench Scale Treatability Study .......1 1.2 Soil Parameters for High Temperature Thermal Desorption

Conceptual Design ........................................................................................3

2 Overview of High Temperature Thermal Desorption Process ........... 5

3 Conceptual Design of the High-Temperature Thermal Desorption System ............................................................................ 8 3.1 Design Parameters........................................................................................8 3.2 System Layout and Specifications.................................................................9

4 References ...................................................................................... 11

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Consortium of International Consultants II

LIST OF TABLES Table 1 Summary of Bench Testing Results for Temperatures equal to 850 de-

grees Fahrenheit (454 degrees Celsius) and Retention Times equal to 20 minutes

Table 2 Weighted Average Concentrations of Analytical Parameters for Terres-

trial Soils Table 3 Summary of Terrestrial Analytical Parameters

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Consortium of International Consultants III

LIST OF FIGURES Figure 1 Proposed High-Temperature Thermal Desorption Process for Kuwait

Contaminated Soils

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Consortium of International Consultants IV

LIST OF ANNEXES Annex 1: High-Temperature Thermal Desorption Component Details Annex 2: Models

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Consortium of International Consultants 1

1 Design Rationale The design of the high temperature thermal desorption system for treating Kuwait petroleum-contaminated soils was based on the following:

1. High Temperature Thermal Desorption Bench Test Results (Volume 2, Appendix E, Annex 2)

2. Weighted Averaged Concentrations of Analytical Parameters for Terrestrial Soils (Table 2)

3. Mass and Thermal Balance (Volume 2, Appendix G, Annex 4, Table 9) 4. Therm-tec General Specifications (Annex 1)

1.1 High Temperature Thermal Desorption Bench Scale Treatability Study The high temperature thermal desorption bench test consisted of treating different soils in a high temperature thermal desorption bench unit at temperatures of 750 degrees Fahrenheit (399 degrees Celsius), 850 degrees Fahrenheit (454 degrees Celsius) and 950 degrees Fahr-enheit (510 degrees Celsius) and at retention times of 10 minutes, 20 minutes and 30 minutes. This set of conditions was repeated three times to establish statistical variability. A total of 174 samples were collected from various locations to support the bench scale study of high temperature thermal desorption. The samples were analyzed for percent moisture, density and British Thermal Units content in addition to total petroleum hydrocarbons. 20 of the samples were subjected to bench scale testing. These 20 samples were selected to be representative of the variety of materials that would undergo high temperature thermal de-sorption treatment. The remaining samples, termed "Supplemental Technology Assessment" samples, were taken to provide a more comprehensive picture of the overall condition of the types of contamination that will be treated by high-temperature thermal desorption. The Supplemental Technology Assessment samples showed a weighted average of approximately 32,000 milligrams per kilogram of total petroleum hydrocarbons. This compares well to a weighted average total petroleum hydrocarbon concentration of approximately 31,000 milli-grams per kilogram for the wet and dry oil contamination and oil-contaminated piles- sam-ples that were collected and analyzed during the field study to define the overall area and de-gree of this contamination. Total petroleum hydrocarbon concentrations in the untreated soils in the bench scale testing ranged from 677 milligrams per kilogram to 431,500 milligrams per kilogram. Both the mean and range of samples used in the high temperature thermal desorp-tion bench scale testing were representative of the materials to be treated. The results of the bench scale testing, presented in Volume 2, Appendix E, Annex 2, show that high temperature thermal desorption can treat all of the types of contamination encoun-tered in both the terrestrial and coastal areas. At a temperature of 850º Fahrenheit (454º Cel-sius) and a retention time of 20 minutes, a full scale high temperature thermal desorption sys-tem can treat the Kuwait contaminated soils to the levels required (no visible contamination). In particular, the results of the portion of the bench testing that are summarized in Table 1 show that at a temperature of 850 degrees Fahrenheit (454 degrees Celsius) and a retention time of 20 minutes, approximately 92 percent of the soil samples whose untreated total petro-

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leum hydrocarbon value was less than 75,350 milligrams per kilogram had a post-treatment total petroleum hydrocarbon concentration of less than or equal to 500 milligrams per kilo-gram. Only three cases of the 39 tested at this temperature and retention time continued to exceed 500 milligrams per kilogram after treatment. There were 23 cases of non-detect (less than or equal to 200 milligrams per kilogram), and the average value of treated soil for all cases, was 268 milligrams per kilogram. This average residual value in the treated soils is substantially below the target goal of 500 milligrams per kilogram of total petroleum hydrocarbons. Table 1 Summary of Bench Testing Results for Temperatures equal to 850 degrees Fahrenheit (454 degrees Celsius) and Retention Times equal to 20 minutes (for soils with pre-treatment total petroleum concentrations less than or equal to 75,350 milligrams per kilogram)

Total Petroleum Hydrocarbons

Total Number of Cases 39

Number of cases that exceed 500 milligrams per kilogram total pe-troleum hydrocar-bons

3 (534, 614, 850)

Number of cases of non-detect

23

Average value of all cases, in milli-grams per kilogram

268

The results in Table 1 were presented for contaminated soils of less than or equal to 75,350 milligrams per kilogram because this approximates the total petroleum hydrocarbon limit which the full-scale high temperature thermal desorption system has been designed (70,000 milligrams per kilogram). Twenty–six cases of sampled soils with a total petroleum hydrocarbon concentration of less than 75,350 milligrams per kilogram were tested at a temperature of 850 degrees Fahrenheit (395 degrees Celsius) and a retention time of 20 minutes for changes in asphaltenes. These samples had pre-treatment asphaltene concentrations that ranged from 926 to 30,600 milli-grams per kilogram. The test results for these 26 cases showed that at this temperature and retention time, the asphaltene concentrations in 25 cases were reduced to less than 500 milli-grams per kilogram, with 15 non-detect results and an average asphaltene concentration of 194 milligrams per kilogram.

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Actually, the results in Table 1 from the High Temperature Thermal Desorption Bench Test provide a conservative estimate of full-scale high temperature thermal desorption system per-formance. The results for the full-scale system are expected to provide improved total petro-leum hydrocarbon desorption efficiency. This is due to the following:

1. Although the bench test reproduces the temperature and retention time of a full-scale system, it does not provide a combustion flame. The presence of a combustion flame in a rotary dryer improves total petroleum hydrocarbon desorption and destruction, and the use of a combustion flame substantially increases the destruction efficiency of asphaltenes.

2. Although the bench scale unit rotates the soil, the rotation of the soil in the full-scale unit provides a higher degree of heat transfer due to “veiling” which causes the hot gases to contact the contaminated soil particles.

The combination of a combustion flame and “veiling”, which are difficult to reproduce in a bench test, will provide greater heat transfer between the soil and the hot gases in the full-scale system, resulting in improved total petroleum hydrocarbon desorption and destruction.

1.2 Soil Parameters for High Temperature Thermal Desorption Conceptual Design In the design of a full-scale high temperature thermal desorption system for treatment of pe-troleum-contaminated soil, soil temperature, and soil retention time are critical parameters. These parameters determine the size and performance characteristics of the high temperature thermal desorption system. For example, the soil retention time required to volatilize/desorb the petroleum compounds in the soil strongly affects the high temperature thermal desorption production rate as shown in the following equation:

[ ] ( ) ( ) ( )1/T R x L x 4 x d x(A)C

2 π=

Where C = high temperature thermal desorption production rate T = Soil retention time R = Material bulk density A = percent loading of soil L = Length of high temperature thermal desorption d = Diameter of high temperature thermal desorption This equation shows that for a final high temperature thermal desorption configuration, the high temperature thermal desorption production rate is inversely proportional to the soil re-tention in the high temperature thermal desorption; the other parameters, which are defined by system configuration and soil properties, are fixed. The soil temperature necessary for the volatilization/desorption of the petroleum compounds strongly affects the energy requirements of the high temperature thermal desorption and the

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gas flow quantities generated in the treatment of the contaminated soil. The system energy requirements in turn determine the fuel consumption of the high temperature thermal desorp-tion; the gas flow quantities determine the size of the high temperature thermal desorption and its required pollution control and energy recovery systems. In the treatment of petroleum contaminated soil, the soil temperature and soil retention time required for desorption are dependent on the following parameters:

• Soil moisture content (percent);

• Soil energy content (kilocalories per kilogram);

• Soil contamination level before treatment (total petroleum hydrocarbons);

• Soil residual contamination level after treatment (total petroleum hydrocarbons); and

• Soil general characteristics such as grain size, clay content, and heat capacity. As shown in Table 2, weighted values of the relevant soil properties required for the concep-tual design (British Thermal Units, total petroleum hydrocarbons, moisture content and dry density) have been calculated. The results shown in this table are based on the extensive sampling and analysis conducted during the Supplemental Technology Assessment, the ana-lytical results for which are summarized in Table 3 and are based on the data in Volume 2, Appendix E, Annex 5. The material quantities presented in Table 2 were obtained from Vol-ume 2, Appendix G, Annex 3. The nominal total petroleum hydrocarbon concentration expected, based on the data in Table 2, is approximately 32,000 milligrams per kilogram. The full-scale high temperature thermal desorption system has been designed for a nominal total petroleum hydrocarbon value of 32,000 milligrams per kilogram. However, it has the flexibility to treat soils with total petro-leum hydrocarbon concentrations from zero to 70,000 milligrams per kilogram, without re-ducing its design feed rate of 100 U.S. tons (about 91 tonnes) per hour. This operational flexibility is based on the use of auxiliary energy for the treatment of soil with less than 32,000 milligrams per kilogram total petroleum hydrocarbons and use of injected water for soils greater than 32,000 milligrams per kilogram.

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2 Overview of High Temperature Thermal Desorption Process

The use of high-temperature thermal desorption for remediation of hydrocarbon-contaminated soils will require the following steps:

1. Development of a soil excavation plan which will allow for the excavation of soils from various sites and ensure that soils transported to the high temperature thermal desorption facility are within the total petroleum hydrocarbon concentrations of the design conditions;

2. Transporting these soils to a high-temperature thermal desorption facility;

3. Storing and preparing the material awaiting treatment at the high-temperature thermal

desorption facility. The feed preparation includes mixing or blending and screening before the desorption process, if necessary;

4. Feeding prepared soils to a high-temperature thermal desorption system;

5. Treating the soils by heating in the system to about 454° Celsius to remove contami-

nants;

6. Cooling the treated soils;

7. Adding water to treated soils to improve handling characteristics;

8. Returning the treated soils to excavated areas; and

9. Backfilling the excavated areas with treated soil. It will be necessary to blend soils prior to treatment to meet the high temperature thermal de-sorption system design condition of treating soils between the range of zero and 70,000 milli-grams per kilogram total petroleum hydrocarbon. The blending of the contaminated soils be-fore they are fed to the high-temperature thermal desorption system is important because:

1. soils with a homogeneous total petroleum hydrocarbon concentration allow the high-temperature thermal desorption system to operate more efficiently without dramatic shifts in gas flow and temperatures, and

2. soils which are homogeneous and approach the nominal design total petroleum hy-

drocarbon value of 32,000 milligrams per kilogram allow the high-temperature ther-mal desorption system to operate with minimum fuel consumption and minimum wa-ter consumption.

This blending will be achieved by:

1. Mixing and blending of soils at the excavation sites. Soils with lower concentrations of total petroleum hydrocarbon will be mixed with soils with higher concentration, to

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reduce the average total petroleum hydrocarbon value of the higher contaminated soils.

2. Additional mixing and blending of soils at the high temperature thermal desorption

site. To ensure that adequate blending of the soils occurs, the high temperature ther-mal desorption system has been designed to include a feed hopper blending system, a pug mill/mixer and a weigh feed hopper to allow for blending of the soils to the nominal design conditions of 32,000 milligrams per kilogram total petroleum hydro-carbon.

In particular, the excavated soils after on site blending will be hauled by trucks to strategi-cally placed treatment facilities to be located near the oil fields. There, the soils will be placed in storage piles. While awaiting treatment the contaminated soil will undergo addi-tional blending. The individual storage piles will be thoroughly mixed by mechanical means (typically a front-end loader) until the pile is homogenous. Based on the average concentra-tion of petroleum hydrocarbons and thermal energy content (British Thermal Units/pound) for each pile, a pre-determined quantity from each of the various storage piles will be placed in a series of hoppers, as shown in Figure 1. These hoppers will then proportionally feed the soils in the desired rates to a common conveyor, which in turn will feed a blender/pug mill where the conveyor soils will be thoroughly mixed to insure a homogenous feed to the high-temperature thermal desorption unit. The high temperature thermal desorption unit is capable of treating contaminated soils which are above or below the nominal design total petroleum hydrocarbon value of 32,000 milli-grams per kilogram to achieve a residual total petroleum hydrocarbon value of 500 milli-grams per kilogram at the design production rate of 100 tons per hour. This flexibility is achieved through the use of auxiliary fuel burners to allow treatment of soil from zero to 32,000 milligrams per kilogram total petroleum hydrocarbon and the use of water injection to allow the treatment of soils with total petroleum hydrocarbon values from 32,000 to 70,000 milligrams per kilogram. It should be noted that the highest concentrations of total petroleum hydrocarbons are found in the wet oil contamination, but these levels will be substantially diluted by the excavation techniques proposed for those areas. Those techniques call for the addition of adjacent dry oil contaminated material to the wet material so that it can be excavated and transported in the solid rather then liquid state. It is estimated this will require about 6 parts dry to 1 part wet material. These will substantially reduce the quantity of high total petroleum hydrocar-bons material to be processed. For the case of the soils between zero and 32,000 milligrams per kilogram, the high tempera-ture thermal desorption auxiliary burners have been conservatively sized to provide sufficient energy for the treatment of soils with zero milligrams per kilogram total petroleum hydrocar-bon concentration for 25 percent of the time, at the approximate cost of $1.12 per United States ton. For the case of soils between 32,000 and 70,000 milligrams per kilogram, the high temperature thermal desorption system has been designed to allow up to 1,200 gallons per hour of water to be injected into the soil at the cost of $0.24 per ton. These costs are in-cluded in the cost estimate of Volume 2, Appendix G, Annex 4. After blending, but before the soils are fed to the high-temperature thermal desorption facil-ity, the soils will be screened for removal of foreign objects, oversized (greater than 2 centi-

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meters) rocks and stones, and large clumps. Soil particles and clumps less than 2 centimeters in size will be fed directly to the high-temperature thermal desorption unit. Stones, rocks, and clumps greater than 2 centimeters in size will be processed in a grinder to reduce their size, and then returned to the pug mill for blending with the soil. The grinder process is im-portant because the large pieces may be high in petroleum hydrocarbons, and the thermal en-ergy content of large pieces of this material could create problems if these pieces were fed directly into the high-temperature thermal desorption unit. The soils, after being screened, will be fed to the high-temperature thermal desorption unit. The high-temperature thermal desorption unit will be an inclined rotary dryer. The material will be fed into the end of the dryer opposite the fuel burner. In this type of system (called a “counter-current feed system”), the contaminated soils will be fed at the “cold” end of the dryer while the treated soils will exit the “hot” end of the dryer. The hot gases will travel in the opposite direction, exiting the rotary dryer at the soil inlet point. The soils will enter at about 32° Celsius and exit at about 454° Celsius. The system combustion gases will exit at 260° Celsius (see Figure 1). These combustion gases will enter a pollution control system. In the pollution control system, particulate emissions will be removed through the use of a mechanical cyclone and baghouse, and organic contaminants will be destroyed in a thermal oxidizer or afterburner that raises the temperature of the gases to around 982° Celsius. The high-temperature gases exiting the afterburner will then be used to generate steam and elec-tricity that can be used to operate the facility, thereby reducing operating costs. The treated soil exiting the high-temperature thermal desorption unit will be sprayed with wa-ter in an enclosed structure to allow for cooling without wind dispersion. The cooled soil may then be stored on site for subsequent return to the excavated area. The counter-current high-temperature thermal desorption system concept provides operating conditions for reaching high soil temperatures with relatively low exit gas temperatures. This is important; the high soil temperatures will provide a higher degree of total petroleum hy-drocarbon removal, while low exit gas temperatures will result in lower capital and operating costs.

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3 Conceptual Design of the High-Temperature Thermal Desorption System

Based on the above discussion and the weighted average British Thermal Units, total petro-leum hydrocarbons, moisture content and dry density from Table 2, a conceptual design exer-cise was conducted to define the best layout and characteristics of a high-temperature thermal desorption system for treating Kuwait hydrocarbon-contaminated soils. This conceptual de-sign was based on the use of mass and thermal balance calculations to define overall system parameters, followed by the application of proven empirical design criteria to establish sys-tem layout and performance. 3.1 Design Parameters The design parameters used in the conceptual design process were:

1. Mass and Thermal Balance:

• Soil Feed Rate = 100 United States tons per hour (~91,000 kilograms per hour) • Soil Moisture Content = The soil moisture content was assumed to be 3 percent.

However, a mass weighted analysis of the soil moisture content from Table 2 yielded a value of approximately 2.08 percent moisture content. Therefore, a de-sign using 3 percent moisture content provides a conservative approach. In actu-ality, the proposed system has been designed with the capability to treat soils with 10 percent moisture content without reducing the feed rate of 100 tons per hour. The 3 percent moisture case represents a nominal design condition.

• Soil Energy Content = 600 British Thermal Units per pound (332 kilo calories per

kilogram). This value was based on the calculated weighted average of all soils (in situ) from Table 2, 538 British Thermal Units per pound (298 kilo calories per kilogram), including the additional volume that must be excavated beyond the neat line. In actuality, the proposed high temperature thermal desorption system has the capability to accept soils with a British Thermal Units value of 1,350 per pound (748 kilo calories per kilogram) but the weighted average of 600 British Thermal Units per pound was used as a nominal case. In addition, the system burners were designed with the capability of treating soils with negligible British Thermal Units content.

• Treated Soil Total Petroleum Hydrocarbon Concentration = 500 milligrams per

kilogram. • System Temperatures

- Soil Inlet Temperature = 32° Celsius (conservative given typical ambient tem-peratures in Kuwait)

- Soil Exit Temperature = 454° Celsius - Air Inlet Temperature = 38° Celsius (conservative given typical ambient tem-

peratures in Kuwait) - Rotary Dryer Exhaust Gas Temperature = 260° Celsius

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- Thermal Oxidizer Inlet Temperature = 232° Celsius - Thermal Oxidizer Exhaust Gas Temperature = 982° Celsius - Heat Loss from System = 10 percent

• System Losses

- 10 percent Heat Loss from Rotary Dryer and Thermal Oxidizer - 25 percent Air Leakage in Rotary Dryer

• Fuel

- Number 2 Diesel Fuel at 25 percent Excess Air

2. Equipment Design Assumptions:

• Rotary Dryer - Soil Retention Time = 20 minutes - Length to Diameter Ratio = 4.0 to 6.0 - Rotary Dryer Fuel = Number 2 (diesel) - Rotary Dryer Excess Air = 25 percent - Dryer Gas Flow Velocity = 350 meters per minute - Maximum Soil Temperature = 510° Celsius - Rotary Dryer Leakage = 25 percent

• Thermal Oxidizer

- Gas Flow Retention Time = >0.5 seconds - Length to Diameter Ratio = 3.0 to 4.0 - Gas Flow Velocity = 19 meters per second - Thermal Oxidizer Excess Air = 200 percent

• Mechanical Cyclone

- High-Temperature Stainless Steel - Removal Efficiency = More than 80 percent for particles more than 10 mi-

crons • Baghouse

- Nomex Bags with Temperature Capability of 246° Celsius - Air to Cloth Ratio = 5.0 to 1.0

• Heat Recovery Boiler

- Boiler Inlet Temperature = 982° Celsius - Boiler Exit Temperature = 232° Celsius - Steam Production: Minimum of 18,000 kilograms per hour

Based on these conditions, a mass and energy balance calculation was performed and is pre-sented in Volume 2, Appendix G, Annex 4, Table 9.

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3.2 System Layout and Specifications The gas flows and energy requirements defined by the mass and energy balance and the design parameters as previously presented were used to conduct an empirical design for each high temperature thermal desorption system component. Therm-tec, Inc., of Tualatin, Oregon, a manufacturer of thermal desorption and incineration systems, was retained to develop general specifications and overall design drawings for the system shown in Figure 1. Therm-tec, Inc. was chosen because it is one of the oldest and most technologically advanced designers, engineers, and manufacturers of special-use incinerators, heat recovery systems, and air pollution control equipment. Therm-tec, Inc.’s, technology in each of these areas is designed to provide the most environmentally safe and practical solution to the needs at hand. Because its equipment is in use throughout the United States and internationally, Therm-tec, Inc., has designed its various systems to meet stringent and frequently updated air pollution control standards in the United States and in other countries. The general specifications prepared by Therm-tec are presented in Annex 1. Annex 1 also contains the electrical power and utility requirements for the conceptual high temperature thermal desorption system. Annex 2 contains general arrangement drawings for the system.

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4 References Brunner, Calvin R., P.E., 1988, Incineration Systems: Selection and Design, Incineration

Consultants, Inc., Reston, Virginia. Dishian, Al, 1991, Operating Costs and Commercial Aspects of Contracting, Remediation

America Seminar. Hawks, Ronald L., April 1991, Considerations in Design and Operation of Thermal Desorp-

tion of Heavy Hydrocarbons, Environmental Quality Management, Inc., Durham, North Carolina, Remediation America Seminar, Orlando, Florida.

Troxler, W., J.J. Cudahy (Zink-Focus Environmental, Knoxville, Tennessee), S.I. Rosenthal

(FW Environmental, Edison, New Jersey), and J.J. Yezzi (United States Environ-mental Protection Agency), September 23-26, 1991, Thermal Desorption of Petro-leum Contaminated Soils, in Proceedings of the 6th Annual Conference on Hydrocar-bon Contaminated Soil, University of Massachusetts, pp. 675-694.

United States Environmental Protection Agency, 1983, Presumptive Remedies: Site Charac-

terization and Technology Selection for CERCLA Sites with Volatile Organic Com-pounds in Soils, 540-F-93-048, Office of Emergency and Remedial Response Hazard-ous Site Control Division 5203G.

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SOURCE: Consortium of International Consultants 2003 ©2003 Consortium of International Consultants

02:001484_KA04_03_05-B1136Fig1.CDR-7/31/03-GRA

Figure 1 Proposed High-Tempature Thermal Desorption Process for Kuwait Contaminated Soils

Contaminated Soilfrom Excavated Site

Contaminated SoilStorage Pile A

Contaminated SoilStorage Pile B

Contaminated SoilStorage Pile C

Contaminated SoilStorage Pile D

Hopper A Hopper B

Blender/Pug Mill

Blender

Cyclone

Hopper C Hopper D

Common Conveyor

Clean SoilStorage Piles

Screening

Grinder

OversizeMaterial

Contaminated SoilFeed SystemHeat Recovery

BoilerThermalOxidizer

Baghouse

H O2

Fuel

Air

CleanSoil

TurbineGenerator

Return Clean Soilto Excavated Sites

Steam

Hot Gases

Stack

Rot eary Dry r

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Table 2: Weighted Average Concentrations of Analytical Parameters for Terrestrial Soils

Parameter UnitsAreas of Dry Oil Contamination

Areas of Wet Oil Contamination -

Sludge Layer

Areas of Wet Oil Contamination -

Below the Sludge Layer

Oil Contaminated

Piles

Oil Trenches, Pipelines, and Spills Total

Quantity1

Neat Line Volumemillion bank cubic meters 24.4777 1.0573 3.5152 14.8215 2.2984 46.1701

Additional Excavation Volumemillion bank cubic meters 9.8380 0.0000 0.7185 0.6443 0.4183 11.2958

Total Volumemillion bank cubic meters 34.3157 1.0573 4.2336 15.4658 2.7167 57.7891

Laboratory Parameters2

Total Petroleum Hydrocarbons3milligrams/ kilograms 28,914 329,296 44,759 49,360 43,533 -

Total Petroleum Hydrocarbons3 milligrams/ tonne 28,914,000 329,296,000 44,759,000 49,360,000 43,533,000 -

Energy Content3British Thermal

Units/pound 365 7540 1456 821 556 -

Energy Content3British Thermal Units/kilograms 805 16,623 3,210 1,810 1,226 -

Bulk Density kilograms/ Liter 1.735 1.0 1.762 1.601 1.621 -

Bulk Densitykilograms/ cubic

meter 1,735 1,000 1,762 1,601 1,621 -

Dry Density4kilograms/ cubic

meter 1,710 778 1,669 1,580 1,554 -

Moisture Content percent 1.44 28.61 5.6 1.33 4.31 -Weighted Average Calculations

Dry Weight of Material in Neat Line Volume tonne 41,865,940 822,130 5,865,254 23,417,765 3,571,818 75,542,908

Dry Weight of Material in Total Excavated Volume5 tonne 58,692,567 822,130 7,064,088 24,435,671 4,221,822 95,236,278

Weight of Moisture in Total Excavated Volume tonne 845,173 235,211 395,589 324,994 181,961 1,982,928Weight of Total Petroleum Hydrocarbons in Neat Line Volume tonne 1,210,512 270,724 262,523 1,155,901 155,492 3,055,152

Total Energy Content in Neat Line Volumemillion British Thermal Units 33,688,986 13,666,152 18,827,058 42,386,039 4,378,228 112,946,464

Weighted Average Total Petroleum Hydrocarbons Concentration6

milligrams/ kilograms - - - - - 32,080

Weighted Average Energy Content7

British Thermal Units/

pound - - - - - 538

Weighted Average Dry Density8tonne/ cubic

meter - - - - - 1.65

Weighted Average Moisture Content9percent - - - - - 2.08

Notes1. Soil volumes based on quantities presented in Volume 2, Appendix G, Annex 3, Table 9.2. Average Total Petroleum Hydrocarbons, Energy Content, Bulk Density, and Moisture Content for each contaminated soil type obtained from Table 3.3. Concentrations based on dry weight.4. Dry density calculated as follows: Dry Density = Bulk Density / (1 + Moisture Content)5. Assume dry density and moisture content of additional excavated material to be equal to that of associated contaminated soil type.6. Weighted Average Total Petroleum Hydrocarbons Concentration = Weight of Total Petroleum Hydrocarbons in Neat Line Volume / Dry Weight of Material in Total Volume.7. Weighted Average Energy Content = Total Energy Content in Neat Line Volume / Dry Weight of Material in Total Volume.8. Weighted Average Dry Density = Dry Weight of Material in Total Volume / Total Volume.9. Weighted Average Moisture Content = Weight of Moisture in Total Volume / Dry Weight of Material in Total Volume.

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Table 3: Summary of Terrestrial Analytical Parameters

Sample Location Statistical Values

Asphaltene (milligrams/ kilogram)

Total Petroleum Hydrocarbons

(milligrams/ kilogram)

Moisture (percent)

Organic (percent)

pH (Standard

Units)

Specific Conductivity

(µmhos/ centimeter)

Bulk Density (kilograms/

liter)

Energy Content (British Thermal

Units/pound)Median: 7,485 45,300 1.12 4.7 7.5 692 1.551 927Average: 7,967 49,360 1.33 6.6 7.5 953 1.601 821Standard Dev.: 2,835 21,515 0.66 5.7 0.8 952 0.141 401Minimum: 4,470 21,800 0.55 1.1 5.8 57 1.383 248Maximum: 13,000 98,100 2.60 20.0 8.7 2,300 1.881 1,310

Median: 4,690 24,300 0.91 3.3 7.8 255 1.724 256Average: 5,532 28,914 1.44 4.1 7.7 612 1.735 365Standard Dev.: 3,881 15,604 1.42 3.0 0.7 892 0.103 360Minimum: 567 8,330 0.10 0.7 4.8 8 1.453 22Maximum: 22,600 105,000 6.92 18.0 8.9 4,770 1.992 1,690

Median: 3,190 30,100 3.29 3.4 7.8 683 1.744 515Average: 9,010 44,759 5.60 6.2 7.6 1,810 1.762 1,456Standard Dev.: 11,966 33,879 8.09 6.1 0.6 3,311 0.150 3,313Minimum: 1,070 12,400 0.19 1.5 6.3 17 1.584 22Maximum: 50,800 155,000 44.80 29.0 8.4 16,800 2.047 17,400

Median: 3,990 37,900 0.78 4.1 6.3 122 1.634 805Average: 6,493 43,533 4.31 4.5 6.4 1,486 1.621 556Standard Dev.: 4,775 11,988 6.14 2.6 0.2 2,402 0.207 463Minimum: 3,490 35,400 0.76 2.1 6.3 77 1.407 22Maximum: 12,000 57,300 11.40 7.3 6.7 4,260 1.820 841

Median: 129,000 283,000 20.00 45.0 6.8 3,180 - 3,650Average: 283,326 329,296 28.61 45.8 6.7 6,165 1.0 7,540Standard Dev.: 234,198 176,904 26.95 27.4 0.6 8,241 - 7,093Minimum: 11,100 57,000 0.60 6.2 5.0 3 - 22Maximum: 770,000 802,000 77.20 91.0 7.7 28,800 - 18,100

Notes

2. The sludge material in the areas of wet oil contamination is a semi liquid, heterogeneous mixture of water, oil and soil. Some of its constituents (e.g., oil) can be expected to be less dense that water), others (e.g., soil particles) will be denser than water. The overall density of the sludge is assumed to be equal to that of water (1.0 kilogram per liter).

1. Analytical data based on samples collected during Supplemental Technology Assessment (see Volume 2, Appendix E, Annex 5).

Areas of Wet Oil Contamination - Sludge Layer2

Oil Contaminated Piles

Areas of Dry Oil Contamination

Areas of Wet Oil Contamination

- Below the Sludge Layer

Oil Trenches, Pipelines, and

Spills

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“oil lakes” monitoring and assessment report ims · 2015-01-04 · “oil lakes” monitoring...

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