2B Green BioEnergy Final Project Aug

Design Report

023-10-001-02

Comprehensive Technology & Project Plan 70 Million Litre per Year

Biodiesel Production Facility Port of Dalhousie, New Brunswick

Prepared for: 2B Green BioEnergy Corporation

P.O. Box 1007 50 Foundry Street, Suite 200

Moncton, New Brunswick E1C 8P2

Prepared By:

Seattle, Washington +1 (206) 462-3600

June 2011

2B Green BioEnergy Corp. June 2011 Port of Dalhousie, NB Table of Contents Comprehensive Technology & Project Plan Page i

TABLE OF CONTENTS

1.00 Introduction 1-1

2.00 EXECUTIVE SUMMARY 2-1

3.00 DESCRIPTION OF PROJECT 3-1 3.01 Process 3-1 3.02 Site and Site Development 3-5 3.03 Buildings and Structures 3-7 3.04 Environmental 3-8 3.05 Permitting 3-8 3.06 Utility Requirements 3-15 3.07 Plant Staffing 3-17

4.00 PROCESS TECHNOLOGY 4-1 4.01 Technology Provider 4-1 4.02 Process Technology 4-3

5.00 PROJECT CAPITAL COST 5-1 5.01 Capital Cost Summary 5-1 5.02 Basis of Capital Cost 5-4

6.00 PROJECT SCHEDULE 6-1

7.00 Attachments 7-1 7.01 Process Flow Diagram 7-1 7.02 Process Design Criteria 7-1 7.03 Site Layout and General Arrangements 7-1 7.04 Material/Energy Balance 7-1 7.05 Equipment List 7-1 7.06 Project Schedule 7-1 7.07 Capital Cost Estimate 7-1 7.08 Information on E3 FullSpectrum 7-1

2B Green BioEnergy Corp. June 2011 Port of Dalhousie, NB Introduction Comprehensive Technology & Project Plan Page 1-1

1.00 Introduction 2B Green BioEnergy Corporation (2B Green) has retained E3 Energy Partners LLC to prepare a Comprehensive Technology and Project Plan for a proposed biodiesel production facility to be located in the Port of Dalhousie, New Brunswick. The 2B Green biodiesel plant will have a capacity of 70 million litres per year. The plant capacity will be built out in modules of 100,000 litres per day, or approximately 35 million litres per year, and can be expanded beyond 70 million litres per year if markets warrant. The plant will be located in a new 9,200 square meter building to be constructed by the Port of Dalhousie. 2B Green will occupy approximately a quarter (2,540 m2) of the building with the remainder of the building to be available for other tenants. Storage tanks will be constructed inside containment berms to the north and west of the building. Loading terminals for biodiesel product and raw materials will be installed for truck, rail and ship. This Comprehensive Technology & Project Plan has been prepared in support of 2B Green’s efforts to develop this project.

Project Contacts

2B Green BioEnergy Corp. P.O. Box 1007 50 Foundry Street, Suite 200 Moncton, New Brunswick E1C 8P2 Anthony Mikalajunas [email protected] +1 (514) 574-7996 Joseph E. Cantini [email protected]

mailto:[email protected]�

mailto:[email protected]�

2B Green BioEnergy Corp. June 2011 Port of Dalhousie, NB Executive Summary Comprehensive Technology & Project Plan Page 2-1

2.00 EXECUTIVE SUMMARY The 2B Green BioEnergy plant will be constructed in the Port of Dalhousie on industrial property leased from the port. The port will also construct the building to house the plant and lease it to 2B Green BioEnergy. The plant will be based on second generation biodiesel processor technology. The plant will consist of two E3 FullSpectrum processor lines of 100,000 litres per day each for an initial combined nameplate capacity of 70 million litres per year. The plant capacity will have the future capability to be expanded in increments of 100,000 litres per day. The plant will have access to rail, truck and ship transportation for receiving of raw materials and shipping of finished product. Storage tanks constructed at the plant site will provide capacity for 4 million litres of raw oil feedstock, 4 million litres of biodiesel, 0.75 million litres of glycerin, 1.0 million litres of methanol and 300,000 litres of catalyst. Plant utilities will include boilers, chillers, compressed air and a nitrogen generation system. Power, water and sewer will be from existing services adjacent to the project site. The cost for this project, through all phases is estimated at $36.9 million.

Project Site Location

2B Green BioEnergy Corp. June 2011 Port of Dalhousie, NB Description of Project Comprehensive Technology & Project Plan Page 3-1

3.00 DESCRIPTION OF PROJECT

3.01 Process

3.01.01 Introduction The proposed project is a new biodiesel production facility owned by 2B Green BioEnergy and scheduled to be constructed in the Port of Dalhousie, New Brunswick. The projected final production capacity of biodiesel is 70 million litres per year (MMLPY) from various feedstocks, including beef tallow and choice white grease.

The E3 FullSpectrum Processor is a batch biodiesel production process. The E3 processors are factory built, skid mounted and function tested before delivery. This means that they are easy to install and that costs for site engineering and the production facility are kept low. A list of the major capital equipment required for the project is shown in Attachment 7.05.

3.01.02 E3 FullSpectrum Processor The E3 FullSpectrum Biodiesel processor is built to industrial design standards. All raw material and biodiesel wetted parts are made of stainless steel to ensure a long lifetime. The process equipment is from established industrial suppliers that can provide local maintenance, parts and support. The processor is compliant with all North American design standards, including UL, FM and CEC requirements.

The E3 FullSpectrum Biodiesel processor is built for batch processing with an advanced processing technique for maximum range in raw material and maximum yield. This means that the processor is very flexible and can handle any raw material that contains fatty acids such as ordinary vegetable oils but also crude palm oil, used cooking oil (UCO, WCO), animal fat and fish oil with a Free Fatty Acids (FFA) content up to 12%. A high level of automation allows the operator to easily switch from one raw material to another by changing processing recipes. The processor can operate both as a stand alone unit or in conjunction with a large number of other units.

The processor is delivered with a performance guarantee specifying quantity and quality which guarantees that the biodiesel produced will meet ASTM D6751 or EN 14214 standards as long as the raw material specifications and operating instructions are followed.

Information on the E3 FullSpectrum processor is provided in Attachment 7.08.

A typical flow diagram for an E3 FullSpectrum processor is shown below:


3.01.03 Biodiesel Chemistry Materials used for producing biodiesel are generally any fats and oils. This specifically is a mixture of triglycerides of different free fatty acids with various carbon chain lengths (typically 10 to 20 carbons in a chain). The transesterification reaction is a reaction between triglycerides and alcohols (typically methanol) under certain conditions to make fatty acid alcohol esters (FAME if using methanol) which is what we call “biodiesel”. This reaction is slow and the reaction rate will be accelerated by adding alkaline catalyst into the reaction mixture. The following diagram shows the alkali-catalyzed transesterification reaction:

O O || || CH2 – O – C – R1 CH3 – O – C – R1 CH2 – OH | O H O | | || | Alkaline || | CH3 – O – C – R2 + 3 HO – C – H ------------> CH3 – O – C – R2 + CH – OH | O | Catalyst O | | || H || | CH2 – O – C – R3 CH3 – O – C – R3 CH2 – OH

(Triglycerides) (Methanol) (Mixture of FAME) (Glycerin)


R1, R2, R3 represent the carbon chain of free fatty acids. Theoretically, 1 part of triglycerides needs 3 parts of methanol to make 3 parts of biodiesel and 1 part of glycerol. The reaction temperature needs to be controlled to around 70-80 ºC. A higher temperature increases the reaction rate to make biodiesel faster, but it also increases the possibility of side reactions which leads to low biodiesel yield and quality.

The produced glycerin is a heavier liquid and it settles out from the biodiesel after the reaction is completed. Biodiesel can then be obtained by separating glycerin by draining or other separation methods, such as centrifuging.

The raw oil should be water-free or at very low water levels, since hydrolysis reactions may occur along with transesterification reaction. Hydrolysis will turn the glycerides into free fatty acids which will react with and consume the alkaline catalyst added into the reaction. This side effect not only reduces the catalyst activation, but also forms soaps which cause many problems in the biodiesel process.

3.01.04 Process Flow Diagram The general process for the entire plant can be visualized with a process flow diagram (PFD), which is included as Attachment 7.01.

The Process Design Criteria that is the basis for this Project Plan is included as Attachment 7.02.

3.01.05 Material Handling and Storage Raw Oil

The feedstock used in the process could be various grades of raw oil or fat.

Raw oil is normally delivered in bulk to the site by tanker truck or rail car and stored in dedicated storage tanks in the tank farm. The feedstock will be automatically transferred from the storage tanks to the processors through a charge pump controlled by the operator.

Biodiesel Product The biodiesel product is normally stored in dedicated storage tanks and collected in bulk by tanker trucks or rail cars. Transfer of product from the process to storage, and from storage to collection vehicles, will be through dedicated loading systems. The system totalizes the flow of the biodiesel and provides overfill and grounding protection for the truck or rail car.

Methanol Fresh methanol is normally delivered in bulk to the site by tanker truck and stored in a dedicated storage tank. A dedicated grounding monitoring system protects the unload system and truck, and redundant level monitoring systems prevent tank overfill. The methanol transfer from storage tanks to processors is a sealed system automated by the processor control system.


Crude Glycerin The crude glycerin is normally stored in a dedicated tank and collected in bulk by tanker trucks. Transfer of crude glycerin from the processor to storage, and from storage to collection vehicles, will be through over-ground process piping.

Sodium Methylate Sodium methylate used in the process is typically sodium methoxides dissolved in methanol. The methylate is purchased from chemical suppliers and normally delivered in bulk by tanker trucks.with a concentration around 30%. Delivery of methylate from tank to processors is automated via over-ground piping.

Additives Additives generally include antioxidants and wintering agents. Addition of antioxidants increases the biodiesel stability for relatively long-term storage. Wintering agents typically reduce the cloud point of biodiesel and increase its cold flow properties.

Additives are purchased from available fuel additives suppliers usually pre-dissolved in biodiesel. Onsite preparation of high concentration additives is another option by adding the additives into biodiesel with a set ratio.

Wastes The waste products from the biodiesel production will be spent filter media, which will need to be changed every 3-5 weeks. Waste will be contained in dedicated storage equipment and transported by road vehicles for disposal off-site at a certified facility.

Further information about the material handling and storage is given in Attachment 7.02 design criteria.

3.01.06 Energy Balance Each biodiesel processor module requires 884 kW of heat from either hot water or steam for the reaction. Additionally, approximately 500 kW of waste heat from the processor is available for tank heating or other low-value heat requirements. The result is that the net process heat requirement for the processors is very low as long as a use is found for the waste heat.

Energy consumption values based on one metric ton of biodiesel produced are shown below:

Electrical Power, kWh 26 Natural Gas, GJ 0.85


Details for the energy balance are shown on the Mass/Energy Balance (Attachment 7.04) and on the design criteria included as Attachment 7.02.

3.01.07 Mass Balance A simplified mass balance for a single processor module is shown in the table below:

Inputs kg/day Outputs kg/day Raw Oil 90,898 Biodiesel 88,100 Methanol 17,596 Methanol (Recovered) 9,427 Sulfuric Acid 440 Glycerin 11,742 Sodium Methylate 405 Other Losses 250 Citric Acid 180

3.02 Site and Site Development The project site is an approximately three hectare site located on the waterfront to the north of the Town of Dalhousie on the south shore of the Bay of Chaleur. The site is today owned by the Port of Dalhousie Inc., a private entity operated by the Longshoremen. The site is presently vacant. It had in the past been used by Brunswick Mines and Xstarata for the storage of ores, i.e., copper, lead and zinc, all of which are mined locally. The lands were cleaned by Xstarata when they vacated the site. The site is bounded to the north by containment disposal cells used to contain dredged materials from the port; to the south across the rail tracks and William Street to the town property. To the east is the lagoon that separates this peninsula from the lands that had been occupied by the pulp and paper mill and to the west are the waters of the Bay of Chaleur. Development of the project site will require cutting and grading of approximately 10,000 cubic meters of soil, all of which will be reused as fill on the project site. Approximately 10,000 cubic meters of clean engineered fill will be brought onto the site for stabilizing and leveling of the developed project area. Development of the project site will primarily be the responsibility of the Port of Dalhousie. The plant area will be graded such that the land rises slightly at the lot boundaries and all rainfall on the property will be collected and treated prior to discharge. The plant yard and tank farm will be paved with concrete suitable for the truck traffic anticipated. Rainfall on the site will be collected and treated appropriately prior to discharge. Rain falling on the building and collected in downspouts will be discharged directly to a stormwater outfall to the north of the property in the drainage basis on this property. Rainwater falling on the truck traffic area will be collected and passed through an oil / water separator prior to discharge into a bioswale to the north. Water falling on the truck and railcar loading areas will be collected in an underground vault which will be pumped out upon confirmation that the contents are not


contaminated. Water falling onto the tank farm area will collect in dry sumps which will be pumped out to the bioswale outfall upon confirmation that the contents are not contaminated. The access road to the plant will tie into existing streets at the southeast corner, which is the intersection of William and George Streets. Rail car access will be provided by installing a switch on the track just to the east of the road intersection, and running a spur along the southern edge of the plant to the tank farm. Ship and barge access will be through an underground pipeline to a loading facility on the West Wharf. The plant site will be fenced with an automated gate. Security cameras and communication equipment to secure the site will be installed. Utilities will be obtained from the various agencies serving the area. Electrical power will be obtained from the local utility who will install their plant transformer at the site boundary. Water for fire suppression and potable uses is available at the southeastern boundry of the site. Sanitary sewage will tie in to existing sanitary conveyance lines. Site general arrangement drawings are shown in Attachment 7.03.


3.03 Buildings and Structures The Port of Dalhousie will construct a new 9,200 square meter building on the site. Approximately one quarter of the building will be occupied by the 2B Green biodiesel plant, and the remainder of the building will be leased to other tenants. The 2B Green portion of the building will house the process equipment, offices, laboratory and control systems. Two tank farm areas will be constructed, one to the north of the building for day tanks and methanol storage, and the other to the west for the main storage tanks. Truck loading and unloading equipment will be installed between the west tank farm and the building. Rail loading/unloading equipment will be installed on the new rail spur at the south end of the west tank farm. The process building to be constructed is generally 61 by 150.8 meters and will be approximately 13 meters high at the roof peak. The eave height of the building will be 7.62 meters. This building will be a metal clad, steel frame building. The building will be designed to meet all aspects of Canada’s National Building Code. The building will have roll-up doors on all sides for installation of the equipment and movement of service materials. Inside the building, about 80% of the 2B Green floor space will be an open area for installation of the process equipment. In this area, the FullSpectrum Processors will be installed along with some of the auxiliary process equipment. The west bay of the building will have a two story office, control room, electrical room and utility area constructed within the main shell. On the ground floor, this bay will have an area devoted to the storage of hazardous materials in totes, an area for installation of process utilities including the plant air compressor, process boiler, chillers and nitrogen supply system, an electrical room for process electrical equipment and a rest room. On its second floor, spaces will be built to house the plant office, the process control room and laboratory. Space will also be provided for parts and maintenance equipment storage. The tank farm for the plant will be built along the north and west sides of the site. The west tank farm will consist of two feedstock tanks, two biodiesel tanks and one glycerin storage tank. The north tank farm will contain a methanol tank, a catalyst tank, two biodiesel holding tanks, and two process vessels. The tank farm area will include space for future day tanks and a future spent methanol tank. All tanks will be installed on a concrete foundation designed for the lateral loads appropriate to the port area. The tank farm area will include secondary containment for all tanks. The secondary containment will be divided into two sections, one to protect the biodiesel and feed stock tanks and one to contain the methanol and catalyst tanks. The main containment area will be surrounded by a wall one meter high with sufficient volume to contain the largest tank plus a 24 hour 100-year rainfall event. The methanol containment


area will be surrounded by a wall 1.5 meters high. The containment structure meets the requirements of Environment Canada for spill protection. Tank Quantitiy Volume, l Height, mm Diameter, mm Retention, day Raw Oil Storage Tank 2 2,000,000 13716 13626 18.4 Biodiesel Storage Tank 2 2,000,000 13716 13626 18.0 Glycerin Storage Tank 1 750,000 9144 10219 14.8 West Tank Farm Tank Quantitiy Volume, l Height, mm Diameter, mm Retention, day Methanol Storage Tank 1 1,000,000 10668 10925 13.6 Catalyst Storage Tank 1 300,000 6706 7547 14.5 Biodiesel Holding Tank 2 500,000 7620 9140 2.2 North Tank Farm Equipment for unloading trucks delivering bulk feedstock and methanol shipments to the site and for loading bulk trucks with biodiesel and raw glycerin will be installed west of the building. A loading rack with a top loading arm including a platform, gangway and safety cage will be installed for loading biodiesel. Additionally, the electrical transformer will be installed outside.

3.04 Environmental In accordance with the requirements of the Canadian Environmental Assessment Act, 2B Green has contracted CBCL Limited to prepare an environmental screening for the proposed project. The Project Description, as the first step in this process, is provided as a component part of the submission to NRCan. Given the industrial context of the site and the information that is available from recent environmental work undertaken in the area, the identified site appears to be an entirely suitable location for the development and operation of the project. No significant environmental impacts are anticipated. 2B Green will therefore be submitting both the environmental screening federally and the environmental registration documentation provincially pursuant to the New Brunswick Clean Environment Act to the pertinent authorities in a matter of weeks. Following release from the federal and provincial environmental assessment processes, 2B Green will seek the required approvals to develop and operate the proposed plant under the New Brunswick Clean Environment Act and the New Brunswick Clean Air Act. At the same time 2B Green will develop and detail an Environmental Management Plan that will include an Environmental Protection Plan for both construction and operation, a management plan for the handling of hazardous materials, a spill protection plan, a groundwater contamination testing and management plan and a contingency plan.

3.05 Permitting 3.05.01 Applicable Codes and Standards


National Building Code of Canada 2005 (NBC)

National Fire Code of Canada 2005 (NFC)

National Plumbing Code of Canada 2005 (NPC)

Model National Energy Code of Canada for Buildings 1997 (MNEC)

2009 Canadian Electrical Code (CEC)

NFPA 30 Flammable and Combustible Liquids Code

NFPA 5000 Building Construction and Safety Code

3.05.02 Facility Description and Use

The project site is currently undeveloped. The proposed project includes the installation of five E3 FullSpectrum biodiesel processor units for the production of fuel grade biodiesel. These processors are automated systems that pump process fluids through a series of vessels where they are heated, cooled, blended and reacted to form biodiesel.

In addition, two tank farms will be built outside the building to house all flammable and combustible fluids used in the process.

The general arrangement of the facility inside and outside of the building is shown on drawing 2310001-GA-002.

A number of flammable and combustible liquids will be used and stored by the facility. The processor input fluids are:

Feedstock which can be vegetable oil or animal fats of various types. This material will differ in combustion properties from lot to lot. The flash point of this material will be no less than 160 °C and typically ranges from 205 °C to 260 °C. Feedstock is a class IIIB Combustible Liquid per NFC and will be stored in tanks in the tank farm.

Methanol, CAS 67-56-1. The flashpoint of methanol is12 °C and its boiling point is 64.7 °C. Methanol is a Class IB Flammable Liquid per NFC and will be stored in tanks in the tank farm.

Sodium Methylate

The process output fluids are:

, CAS 124-41-4 as a 30% solution of methanol. This material has essentially the same flash point and boiling points of methanol and is a Class IB Flammable Liquid per NFC. Sodium Methylate is also referred to as “catalyst” and will be stored in a tank in the tank farm area.

Biodiesel, CAS No. 67784-80-9. Biodiesel is a mixture of a variety of the methyl esters of the fatty acid chains derived from the feed stock. It has a flash point of 130 °C and is a Class IIIB Combustible Liquid per the NFC. Biodiesel will be stored in the tank farm area.


Crude Glycerin

, CAS 56-81-5. Crude glycerin has a flash point of 160 °C and is a Class IIIB Combustible Liquid per the NFC. Glycerin will be stored in the tank farm area in a dedicated tank.

3.05.03 Building Occupancy Classification

Each processor is a sealed system with no open tanks or vessels which contain flammable or combustible liquids. The piping system for the facility is entirely closed.

The amount of Flammable Liquid present in the processors at any one time is 31 litres per processor or 156 litres total. This is less than the permissible amount of Class I Flammable Liquids per the NFC.

The amount of Combustible Liquid present in the processors at any one time is approximately 50,000 litres each or 250,000 litres of Class IIIB Combustible Liquid. This is less than the permissible amount of Class IIIB Combustible Liquid in a sprinklered building per the NFC.

No other materials presenting a physical or health hazard are to be used within the building. Therefore, the occupancy meets the requirements of F-1 Factory Industrial Moderate-hazard per the NBC.

3.05.04 Building Construction

The building structure will consists of steel frames with metal cladding, Type II B Construction. The interior of the building shell will be insulated, but otherwise unfinished.

Interior offices, laboratory, equipment rooms and miscellaneous storage areas will be constructed within the building.

A hazardous material storage area will be constructed within the building of concrete blocks with a steel and concrete ceiling. It will have a total floor area of 395 m² and fire rated walls and ceiling at 3 hours.

An electrical equipment room will be constructed within the building with walls and ceiling fire rated at 2 hours.

The overall building dimensions are 61 m x 150.8 m with a total floor area of 9,200 m², of which 2B Green will occupy approximately one quarter. In the 2B Green area there will be some offices occupying a mezzanine area of approximately 385 m² above the ground floor equipment rooms.

Miscellaneous storage area exists within the building of 500 m².

Restrooms occupy 46 m².

The building will be fully sprinklered throughout.

Details of the building are shown on drawings 2310001-GA-010, 020 & 021.


3.05.05 Tank Farm Construction

The tank farms for the facility are located to the north and west of the building as shown on drawing 2310001-GA-002.

Each tank farm area is constructed with concrete floor and containment walls. Two separate containment areas are constructed for methanol and catalyst. The methanol containment area is 416 m², the catalyst containment area is 242 m², the north tank farm containment area is 908 m² and the west tank farm containment area is 1,640 m². The volumes of the containment areas are sufficient to contain the volume of the largest tank plus the 24-hour maximum rainfall.

3.05.06 Zoning

The site zoning is heavy industrial.

3.05.07 Occupant Calculations

Occupants calculated per NBC

Industrial Areas - one person per 10 sq m

Business Areas - one person per 10 sq m

Gross building area - 4,600 sq m - calculated building occupants = 460

Actual Building Occupants (See Section 3.05.10) = 58 (Posted Maximum = 100)

Restroom Fixture Requirements per NPC

Criteria Requirement Provided Meets

Requirement

Water Closets - Male 100 2 4 Yes

Water Closets - Female

100 2 3 Yes

Lavatories - Male 100 2 2 Yes

Lavatories - Female 100 2 2 Yes

Showers none required for industrial occupancies (see note below)

Drinking fountain Not required for industrial occupancy

Service Sinks 1 1 Yes

Note: One shower will be provided as part of the employee’s amenities. Additional safety showers will be provided in the plant to meet personnel safety requirements.


3.05.08 Building Ventilation

Building ventilation design is based on API (American Petroluem Institute) Recommended Practice 500 – “Recommended Practice for Classification of Locations for Electrical Installation at Petroleum Facilities Classified as Class 1, Division 1 and Division 2”. The design criteria is 15.8 m³/hr of ventilation per gross square meter (1 cfm per sq. ft) of building area.

This criteria exceeds the requirements of the NBC and are required for process safety and personnel health.

The building will be designed to meet the energy efficiency requirements of the MNEC.

3.05.09 Code Limitations and Requirements

Building Area:

- per National Building Code - Unlimited

Fire sprinklers throughout the building, clear open yards are provided around building

Distance to property line that can be built upon (BD – biodiesel, FS – feedstock):

- per National Fire Code Requirement Provided Meets Requirement

From process building 6 m 30+ m Yes


From methanol (Class IB) tanks 6 m 30+ m Yes


From BD/FS (Class IIIB) tanks 3 m 30+ m Yes Distance to public way or important building:


From process building 3 m 30+ m Yes


From methanol (Class IB) tanks 1.5 m 30+ m Yes


From BD/FS (Class IIIB) tanks 1.5 m 30+ m Yes


Shell to Shell Spacing: - Between methanol (Class IB) tanks per NFPA – 1/6 the sum of adjacent tank diameters.

Requirement Provided Meets Requirement

1.8 m 7.5+ m Yes - Between BD/Feedstock tanks per NFPA - 1/6 the sum of adjacent tank diameters.

Requirement Provided Meets Requirement

4.5 m 13.4 m Yes Electrical:

- Areas where Class I liquids are handled are required to be classified per the CEC.

Areas within the building where flammable vapors can exist have been classified as Class I, Division 1 Group D with due regard for the operation of the equipment and building ventilation.

Piping:

- Piping systems are required to be suitable for the working pressures and structural stresses to be encountered by the piping system per the NFC.

Piping systems are designed, fabricated, installed, inspected and tested in conformance with the requirements of ASME (American Society of Mechanical Engineers) B31.3 Process Piping as per the NFC.

3.05.10 Code Requirements

Classification of Occupancy and Hazard of Contents -

The building is classified as Industrial per the NFC

The contents are likely to burn with moderate rapidity or to give off a considerable amount of smoke and are classified as Ordinary Hazard per NFC

The occupancy is further sub-classified as Special Purpose Industrial Occupancy per NFC due to ordinary industrial operations being conducted in a building with a relatively low density of employee population with much of the area occupied by machinery or equipment. Occupant Load -

The NBC states that the occupant load is to be the maximum probable number of occupants present at any one time. This is calculated as follows:

Operators 11


Supervisors 5

Maintenance 18

Business / Secretarial 22

Visitors 2

Total 58

Arrangement of Exits -

For special purpose industrial occupancies in fully sprinklered buildings, exits must be separated by 1/3 of the diagonal dimension of the building per NFC. The overall occupied area dimensions are 75.4 m x 61 m. One third of the diagonal dimension is 26 meters.

The limit for common paths of travel per NFC is 30 meters.

For dead end corridors the limit is 6 meters.

Maximum travel distance to an exit per NFC is 120 meters. All travel distances within the building are less than120 meters from the nearest exit.


3.06 Utility Requirements Following are the estimated utility requirements for the plant site:

3.06.01 Electricity Electricity is consumed by the E3 FullSpectrum biodiesel processor to power the motors on the process pumps, process instrumentation and compressors, and at the tank farm to power the motors on the loading and unloading pumps and instrumentation.

Typical electricity consumption for one FullSpectrum processor is listed below. 1) Processor - 801,710 kWh/yr 2) Tank Farm - 17,125 kWh/yr

a. Feedstock - 7,110 kWh/yr b. Biodiesel - 7,110 kWh/yr c. Methanol - 1,244 kWh/yr d. Catalyst - 325 kWh/yr e. Glycerin - 1,333 kWh/yr

3) Total Electricity - 835,957 kWh/yr

The corresponding electricity consumption of the proposed 2B Green 70 MMLPY biodiesel plant is then:

1) Processors (2) - 1,603,420 kWh/yr 2) Tank Farm - 34,250 kWh/yr

a. Feedstock - 14,220 kWh/yr b. Biodiesel - 14,220 kWh/yr c. Methanol - 2,488 kWh/yr d. Catalyst - 650 kWh/yr e. Glycerin - 2,666 kWh/yr

3) Total Electricity - 1,671,914 kWh/yr 3.06.02 Nitrogen Nitrogen gas is consumed by the tank farm vessels to provide blanket gas for safety and to supply vapor dilution for methanol removal from biodiesel in the process.

Typical nitrogen consumption is about 113 LPM at 6.2 bar. Based on continuous operation at 24 hours a day and 350 days a year, the yearly nitrogen consumption requires 57,053 m³/yr, roughly 421,336 kg/yr. If liquid nitrogen is purchased, the liquid nitrogen volume requires 521,456 litres/year.

3.06.03 Compressed Air Compressed air is supplied for instrumentation control across the plant. A separate air compressor system is proposed for this 70 MMLPY biodiesel plant with the capacity of 0.4 LPM at 8 bar.


3.06.04 Utility Water Utility water consumption is for housekeeping use only. Process consumption of utility water is zero.

3.06.05 Potable Water Potable water will be used for restrooms and drinking water. The estimated potable water consumption is 3,300 litres per day.

3.06.06 Sanitary Sewer The sanitary sewer will be connected to the restrooms, utility sinks and laboratory drains only. The estimated sewer flow from all of these sources is 1,350 litres per day.

3.06.07 Boiler Fuel The boiler is used to provide sufficient heat for the process to the FullSpectrum processors through a circulating hot water system. At the tank farm hot water is also used to provide heat to warm up the feedstock before it can be transferred to the processor. The generated heat is also used for maintaining the tank storage temperature of feedstock, biodiesel, and glycerin. Methanol and Catalyst do not require any heat to keep the fluid liquid, even in cold weather.

Typical energy requirement for the boiler and tank farm warming of a single FullSpectrum processor system is listed below.

1) Processor - 4,410 GJ/yr 2) Tank Farm - 1,167 GJ/yr

a. Feedstock Storage Tanks - 252 GJ/yr b. Biodiesel Storage Tanks - 642 GJ/yr c. Feedstock Holding Tanks - 44 GJ/yr d. Biodiesel Holding Tanks - 119 GJ/yr e. Glycerin Storage Tanks - 113 GJ/yr

3) Total Energy Needed - 6,747 GJ/yr

Either on-site produced biodiesel or purchased No. 2 diesel could be used for the boiler fuel. Typical energy density of No.2 Diesel fuel and biodiesel fuel are around 33.2 and 31.9 MJ/kg, respectively. If the heat efficiency of boiler is 80%, the average boiler fuel consumptions to each heating purpose for a single processor are:

No.2 Diesel Fuel Biodiesel Fuel 1) Processor 173,835 kg/yr 180,696 kg/yr 2) Tank Farm 44,004 kg/yr 45,740 kg/yr

a. Feedstock Storage Tanks 9,467 kg/yr 9,840 kg/yr b. Biodiesel Storage Tanks 24,154 kg/yr 25,106 kg/yr c. Feedstock Holding Tanks 1,646 kg/yr 1,710 kg/yr d. Biodiesel Holding Tanks 4,510 kg/yr 4,690 kg/yr


e. Glycerin Storage Tanks 4,227 kg/yr 4,394 kg/yr 3) Total Fuel Needed (Mass) 217,839 kg/yr 226,436 kg/yr (Volume) 256.29 m3/yr 257.13 m3/yr

The corresponding boiler fuel consumption of the proposed 2B Green 70 MMLPY biodiesel plant is then:

No.2 Diesel Fuel Biodiesel Fuel 1) Processors (2) 347.7 Tonnes/yr 361.4 Tonnes/yr 2) Tank Farm 88.0 Tonnes/yr 91.5 Tonnes/yr

a. Feedstock Storage Tanks 18.9 Tonnes/yr 19.7 Tonnes/yr b. Biodiesel Storage Tanks 24.3 Tonnes/yr 50.2 Tonnes/yr c. Feedstock Holding Tanks 3.3 Tonnes/yr 3.4 Tonnes/yr d. Biodiesel Holding Tanks 9.0 Tonnes/yr 9.4 Tonnes/yr e. Glycerin Storage Tanks 8.4 Tonnes/yr 8.8 Tonnes/yr

3) Total Fuel Needed (Mass) 435.7 Tonnes/yr 452.9 Tonnes/yr (Volume) 512.6 m3/yr 514.3 m3/yr

3.07 Plant Staffing Estimated plant staffing is shown in the table below:

Owner's Personnel Shifts Per Shift Number Annual $ Weekly $ Management:

Plant Manager

1 95,000 2,338 Operations Manager

1 85,000 2,092

Technical Manager

0.5 75,000 923 Engineering/Maintenance

Manager

0.5 72,000 886 Environmental

Manager

0.5 68,000 837 Safety Manager

0.5 55,000 677

Shipping/Procurement

1 48,000 1,182 Administrative 1 38,000 935

Operations Department

Shift Supervisors 4 1 4 52,000 5,120 Operators 4 2 8 43,000 8,468

Maintenance

Day Shift Personnel

Mechanical

1 45,000 1,108 E&I

1 42,000 1,034

Programmer/IT 1 42,000 1,034 Technical

Lab Supervisor

1 44,000 1,083 Shift Testers 4 1 4 38,000 3,742 Day Testers 1 35,000 862

Total Staff 27 $ 32,320


The table above is fairly typical for staffing for a plant of this type. This level of staffing will provide 15 people working during a normal day shift and 4 people working evening, graveyard and swing shifts, for a total of 27 employees. During commissioning, start-up and plant outages additional labor should be planned on from engineering and contract resources.

2B Green BioEnergy Corp. June 2011 Port of Dalhousie, NB Process Technology Comprehensive Technology & Project Plan Page 4-1

4.00 PROCESS TECHNOLOGY

4.01 Technology Provider

E3 Energy Partners delivers industry-leading chemical engineering, process scale-up, full production facility design and project management services for next-generation biodiesel technologies and projects. We provide our clients with leading-edge solutions for new and existing biodiesel facilities that are installing, expanding or upgrading their process technology with advanced pretreatment, processing and purification systems—ensuring that our clients gain a competitive advantage in today’s rapidly changing biodiesel industry.

We deliver modular solutions to treat and utilize the full spectrum of biodiesel feedstock: High and Ultra-High FFA Feedstock Pretreatment

• Acid esterification for feedstocks up to 20% FFA • Glycerolysis for feedstocks from 20% to 100% FFA • Processing of animal fats; waste vegetable oil; corn oil from ethanol plants;

yellow, brown and trap grease; and PFAD • High-efficiency conversion from 5 to 30 MMGPY • Designs for new and existing biodiesel process lines

Our distillation and fractionation solutions enable existing and new biodiesel production facilities to:

Advanced Purification and Fractionation

• Improve biodiesel cold flow properties • Meet ASTM and EN standards • Produce multi-grade biodiesel that can be sold in multiple regions and

temperature ranges • Export non-virgin oil biodiesel to Europe and other markets • Produce ultra-pure biodiesel for premium markets worldwide

We provide modular and large-scale biodiesel process and facility design: Turnkey Process and Facility Design

• Pre-engineered, multi-feedstock biodiesel solutions • Custom-designed biodiesel facilities from 10 to 300 MMGY • Continuous flow, waterless processes and methanol recovery • High energy efficiency and fully automated controls

Our engineering services are dedicated to developing next-generation biodiesel solutions and systems capable of utilizing all possible biodiesel feedstocks—including agricultural, industrial and livestock waste—to create the highest-quality product worldwide. This requires a deep focus on process definition, kinetics, mass-balance and economics. As the biodiesel industry evolves, we remain at the forefront of integrating technology,


operations and economic viability. Industrial biodiesel solutions are complex endeavors, requiring the strength and flexibility of an engineering team that has solved some of the most complicated issues in making biodiesel production competitive and profitable. With decades of experience in energy and biomass—from our early roots in petrochemical and pulp & paper, to our expertise in next-generation biodiesel, cellulosic ethanol and biogas—we provide clients with a level of expertise that is unmatched in our industry.

In addition to our engineering design and study expertise, we bridge the gap between technology and business with the following professional services:

Specialty Services

• Owner’s Representation E3 Energy Partners works on behalf of project developers and government entities as expert counsel to ensure that projects are delivered as designed and within budget.

• Due Diligence We assist venture capital and private equity firms in reviewing and assessing the feasibility and value of biomass-toenergy projects and technologies.

• Feasibility Studies We help determine the technological and financial feasibility of potential project and technology opportunities for project developers.

• Grant Authoring and Support We author and contribute to Department of Energy and USDA grant proposals, and have a successful track record of helping secure awards up to $30 million.

• Licensed Technologies We have developed proprietary technologies—including pretreatment for poor-quality fats and oils, distillation of biodiesel, and other process improvements—that we license to global partners to increase the spectrum of suitable feedstocks and quality of final product.

For more than 25 years, our team has partnered with project developers, industrial companies and renewable energy technology providers around the world to create, scale up and deploy new energy technologies and turnkey facilities. With hands-on experience in North America, South America, Europe and Asia, we pride ourselves on our flexibility and responsiveness in supporting clients and partners across a wide spectrum of new energy projects. Our clients trust us to provide straight answers and innovative solutions. Headquartered in the Pacific Northwest, E3 Energy Partners was founded to deliver focused expertise in next-generation renewables, process scale-up and detailed design.

Global experience, local expertise


4.02 Process Technology The E3 FullSpectrum biodiesel process is a batch process designed for maximum flexibility in processing a wide variety of oils and fats into biodiesel. The process is developed around modular units of 100,000 litres per day that can be paralleled to provide a variety of plant sizes and configurations. The process can be customized with a variety of pre-treatment and purification options that allow acceptance of low quality oils with the capability to process them into high quality biodiesel with relatively high yields. The key advantages to the process are:

• Ability to blend and process a wide variety of oils and fats. • Batch processing for maximum flexibility • Modular design for managed growth • Water-free purification • High level of energy integration & methanol recovery • Post-treatment to fine tune properties and provide better cold-flow properties. • Highly automated with low consumable and operating costs per unit produced

Options:

• Degumming, drying & filtering feedstock oils & fats • Feedstock pretreatment from 0 to12% and / or 12% to 100% FFA • Integrated FOG rendering (trap to brown grease) • Advanced purification via distillation

Process Item Description Basic Plant

Basic Plant Components Tank Farm, Rail Load/Unload, Truck Load/Unload, Pre-Treatment, Transesterification, Methanol Recovery, Purification, Vent Recovery, Thermal Driver, and Utilities.

Plant Turndown 5:1 Plant Single Line Size (Module)

100,000 litres per day; 26,420 gallons / day 16,000 MT / yr.; 9.2 MMGY

Number of Lines One to Six Yield 96% Minimum

Basic Plant Process Details: Oil Pre-Treatment Oil is treated to reduce free fatty acids, dried to

remove water, and filtered to remove solids. Acid esterification is used for FFA below 12%, and glycerol esterification is used for FFA levels from 12 to 100%.


Process Item Description Transesterification The pre-treated oil is processed in a single stage batch

reactor, using high-shear mixing. The use of high shear mixers allows for a faster initial reaction rate, and quicker separation of glycerol. The process also allows for re-treatment of off-spec product, and recycling of glycerol for catalyst use reduction.

Catalyst A sodium methylate solution in methanol is used as the transesterification reaction catalyst. Acid esterification uses a sulfuric acid catalyst, and glycerol esterification uses a metal oxide catalyst.

Methanol Recovery Methanol is recovered through flash evaporation. Methanol is recovered separately from the acid esterification, transesterification and glycerin recovery stages..

Methanol Rectification Recovered methanol vapor is rectified in a packed column to separate water, and provide purified methanol back to the process.

Purification Purification options include processing of the biodiesel through an ion-exchange column to remove impurities, and distillation for biodiesel from low quality feedstocks that might have difficulty meeting ASTM specifications..

Post-Treatment A cold-filtering system provides a biodiesel that will meet ASTM cold-soak specifications.

Thermal Driver The high temperatures required for the glycerol esterification pre-treatment process, and the distillation purification make hot oil the most cost effective thermal source for the plant. Steam is an option for the portions of the process that do not require higher temperatures.

Energy Integration The energy from the plant hot streams have been closely matched to cold streams for pre-heating. The plant heat is tightly integrated to provide maximum efficiency.

Vent Gas Collection All tank and process vents are collected and combusted in the hot oil burner.

Safety Plant process areas are identified by hazard classification, and all energy sources within that area are either explosion-proof, or intrinsically safe.

Feedstock: Oil Type Any filtered, degummed oil or fat, either recycled or

virgin.


Process Item Description Free Fatty Acid (FFA), Max. %

No limit on FFA content (depending on pre-treatment option selected)

Water Content, Max. % 5% Unsaponifiables, Max. % No limit, but will reduce yield. Phosphorus, Max. 50 PPM Sulfur, Max. 25 PPM (Optional sulfur treatments are available for

higher levels) Yield (1 MT pure oil): (Glycerol esterification pre-treatment with ion-

exchange purification) Biodiesel, kg 980 Crude Glycerol, kg 136

Utilities (per 1 MT Product): Electrical Power, kWh 26 Natural Gas, GJ 0.85 Plant Water, litre 0 Compressed Air, Nm³ 6.2 Nitrogen, Nm³ 2.2

Consumables (per 1 MT Product):

Methanol. kg 107 Sodium Methylate, kg 4.6 Ion Exchange Resin, kg 1

Emissions (per 1 MT Product): Methanol Vapor, kg 0.00894 Water Vapor, kg 21.44 Solids, kg 5.30

2B Green BioEnergy Corp. June 2011 Port of Dalhousie, NB Project Capital Costs Comprehensive Technology & Project Plan Page 5-1

5.00 PROJECT CAPITAL COST The plant installation will include two processor modules for an annual capacity of 70 million litres per year. The capital cost for this project is sumarized below:

Total Plant Capital Cost (2 Processors) $ 36,926,874 A summary of the capital costs is shown below. Estimate details are included in Attachment 7.07.

5.01 Capital Cost Summary Plant Capital Cost (2 Processors)

% of Total

Labor Manhours

Labor Costs

Material Costs

Equipment Costs

SubContract Costs Total Costs

Site Work 6.5%

11,686 $730,375 $1,537,810 $0 $125,000 $2,393,185

Civil/Structural 15.9%

25,133 $1,755,540 $4,122,925 $0 $0 $5,878,465 Process 41.0%

14,230 $960,241 $502,941 $13,659,737 $0 $15,122,918

Mechanical 1.2%

2,636 $178,662 $71,030 $193,925 $0 $443,617 Piping 6.9%

17,934 $1,291,212 $1,244,700 $0 $0 $2,535,912

Electrical 5.1%

11,820 $809,684 $1,060,670 $0 $0 $1,870,354 Instrumentation 2.8%

5,009 $393,061 $140,796 $501,286 $0 $1,035,143

Contractor OH&P 3.5%

$1,296,401

Indirect Costs 9.3%

$3,422,920

Contingency 7.9%

$2,927,959

Total Cost 100.0% $36,926,874


In the following sections the plant capital costs are broken out by how they relate in the categories of Production Material, Building, Leasehold Improvements and Infrastructure.

5.01.01 Production Material The production material costs include process equipment, tanks, and systems directly related to the production of biodiesel.

Production Material

% of Total

Labor Manhours

Labor Costs

Material Costs

Equipment Costs


Site Work 0.0%

- $0 $0 $0 $0 $0


- $0 $0 $0 $0 $0 Process 94.7%

14,230 $960,241 $502,941 $13,659,737 $0 $15,122,918

Mechanical 0.0%

- $0 $0 $0 $0 $0 Piping 0.0%

- $0 $0 $0 $0 $0

Electrical 0.0%

- $0 $0 $0 $0 $0 Instrumentation 3.3%

2,373 $192,198 $71,766 $255,785 $0 $519,749


$324,100

Indirect Costs 0.0%

$0

Contingency 0.0%

$0

Total Cost 100.0% $15,966,767 Leasehold Improvement Costs

% of Total

Labor Manhours

Labor Costs

Material Costs

Equipment Costs


Site Work 0.0%

- $0 $0 $0 $0 $0


25,133 $1,755,540 $4,122,925 $0 $0 $5,878,465 Process 0.0%

- $0 $0 $0 $0 $0

Mechanical 1.4%

436 $30,162 $1,980 $193,925 $0 $226,067 Piping 0.0%

- $0 $0 $0 $0 $0

Electrical 0.0%

- $0 $0 $0 $0 $0 Instrumentation 0.0%

- $0 $0 $0 $0 $0


$324,100

Indirect Costs 0.0%

$0

Contingency 0.0%

$0

Total Cost 40.3% $6,428,632

5.01.02 Building


The building costs relate to tenant improvements to the building and surrounding grounds, that will likely stay with the building should the plant process be relocated. These costs do not include the cost of the building itself, which is understood to be provided by the Port of Dalhousie. These costs do include paving, utilities, fencing, security, fire protection, building mechanical systems, HVAC, lighting, and civil/concrete work related to the building structure and grounds.

Building

% of Total

Labor Manhours

Labor Costs

Material Costs

Equipment Costs


Site Work 13.8%

406 $25,375 $1,079,45

0 $0 $125,000 $1,229,825 Civil/Structural 0.0%

- $0 $0 $0 $0 $0

Process 0.0%

- $0 $0 $0 $0 $0 Mechanical 2.4%

2,200 $148,500 $69,050 $0 $0 $217,550

Piping 19.6%

13,059 $940,212 $801,270 $0 $0 $1,741,482 Electrical 13.1%

7,669 $525,303 $640,468 $0 $0 $1,165,770

Instrumentation 0.1%

74 $5,639 $1,890 $3,501 $0 $11,030 Contractor OH&P 7.3%

$648,201

Indirect Costs 23.6%

$2,097,895

Contingency 20.1%

$1,794,536

Total Cost 100.0% $8,906,288

5.01.03 Infrastructure The infrastructure costs relate to improvements to the Port of Dalhousie infrastructure as a whole. These include installation and improvements to roads, wharves, rail loading terminals, truck loading terminals, ship loading terminals, and installing a new pipeline from the new warehouse to the wharf for ship/barge loading.

Infrastructure

% of Total

Labor Manhours

Labor Costs

Material Costs

Equipment Costs

SubContract Costs

Total Costs

Site Work 20.7%

11,280 $705,000 $458,360 $0 $0 $1,163,360


- $0 $0 $0 $0 $0 Process 0.0%

- $0 $0 $0 $0 $0

Mechanical 0.0%

- $0 $0 $0 $0 $0 Piping 14.1%

4,875 $351,000 $443,430 $0 $0 $794,430

Electrical 12.5%

4,152 $284,381 $420,203 $0 $0 $704,584 Instrumentation 9.0%

2,562 $195,224 $67,140 $242,000 $0 $504,364


$0


% of Total

Labor Manhours

Labor Costs

Material Costs

Equipment Costs

SubContract Costs

Total Costs

Indirect Costs 23.6%

$1,325,025

Contingency 20.1%

$1,133,424

Total Cost 100.0% $5,625,187

5.02 Basis of Capital Cost The capital cost above has been developed on the following basis: Contractor Quotes. Fixed price costs were obtained from local contractors. Process Equipment. Process equipment costs were based on vendor fixed price quotations. Quotations were submitted by qualified vendors against engineered equipment specifications. Quotations were obtained in May 2011 and are valid for 60 days. Buildings and Structures. The buildings and structural work cost is based on vendor quotes and contractor take-off. The metal building shell cost is based on vendor quotations obtained from the architectural drawings of the building. The metal building vendor is responsible for the design of the building to meet the site requirements, supply of the building roof, siding and structural systems and erection on the owner’s foundations. The cost of foundations and other concrete work is based on contractor take-offs from engineering drawings and specifications. The cost of the internal structure of the metal building shell are based on contractor take-offs from engineering drawings and specifications. Site work. Site work is based on contractor estimats for the work specified. The contractor estimate was prepared from completed civil drawings based on the site plan, survey and plant arrangement. Piping. Piping cost is based on contractor estimates for material, fabrication and installation. The contractor estimate was prepared from a completed set of P&ID’s for the process and utility systems, piping orthographic plans and sections and a complete piping specification. Electrical. The costs for electrical equipment is based on vendor quotations for equipment shown on the electrical single line diagram and in the equipment list. Motors will be provided by equipment suppliers according to the appropriate specification. Costs for installation materials and labor are based on contractor estimates. Process Control. The cost for process control equipment is based on vendor quotations for all instruments shown on the P&ID’s and Instrument List. These quotations were obtained in January 2011 and are valid for 60 days. Small components of the instrumentation system were estimated based on list prices. The control system for the plant is part of the FullSpectrum Processors. Cost for installation materials and labor are based on contractor take-offs.


Construction Schedule. The prices and cost used in the estimate are current prices as of January, 2011. No allowance has been made for escalation or costs due to delay or deferral of the construction.

2B Green BioEnergy Corp. June 2011 Port of Dalhousie, NB Project Schedule Comprehensive Technology & Project Plan Page 6-1

6.00 PROJECT SCHEDULE A detailed project schedule that includes the project critical path is included in Attachment 7.06. Key milestones for the project are shown in the table below:

Milestone Task Project Start

Completion Date September 2011

Engineering Complete December 31, 2011 Construction Start December 6, 2011 Building Complete (Separate Contract) December 24, 2011 Mechanical Completion February 17, 2012 Processor 1 Start-up February 28, 2012 Processor 2 Start-up May 10, 2012 Plant Operating at Full Capacity July 27, 2012 Completion of Warranty Runs August 24, 2012

The project schedule is based on a fairly aggressive project timeline that includes the following key elements:

• Delivery of the Processors • Construction of the building within 4 months of project start. • Construction of the Tank Farm complete within 8 months of project start.

2B Green BioEnergy Corp. June 2011 Port of Dalhousie, NB Attachments Comprehensive Technology & Project Plan Page 7-1

7.00 Attachments

7.01 Process Flow Diagram

7.02 Process Design Criteria

7.03 Site Layout and General Arrangements

7.04 Material/Energy Balance

7.05 Equipment List

7.06 Project Schedule

7.07 Capital Cost Estimate

7.08 Information on E3 FullSpectrum

2B Green BioEnergy Corp. June 2011 Port of Dalhousie, NB Attachments Comprehensive Technology & Project Plan

ATTACHMENT 7.01


ATTACHMENT 7.02

Page 1 of 23

Project No: 023-10-001-02Created on: 6/27/2011Revision: 0Revised on: 6/27/2011

Amount Unit Amount Unit

Plant ProductionOperating Mode Batch BatchOperating Days 350 Days 350 DaysBatches per Day per Processor 2 Batches 2 BatchesBatch Production 100,000 Liters 26,417 GallonsTotal Number of Processors 2 18 Annual Production, in Volume @ 25 °C 70,000,000 Liters 166,428,393 Gallons

Feedstock ReceivingRaw Oil from Tanker Truck to Feedstock Tank (T-711), Voluemtric Flow, P-722 946 LPM 250 GPMRaw Oil from Tanker Truck to Feedstock Tank (T-711), Mass Flow, P-722 860 Kg/Min 1,895 Lbs/MinRaw Oil from Tanker Truck to Feedstock Tank (T-711), Temperature, P-722 40 ºC 104 ºFRaw Oil from Tanker Truck to Feedstock Tank (T-711), Pressure, P-722 1.0 atm 14.7 PsiaRaw Oil from Tanker Truck to Feedstock Tank (T-711), Density, P-722 0.908 Kg/Liter 7.580 Lbs/GalRaw Oil from Tanker Truck to Feedstock Tank (T-711), Viscosity, P-722 25.8 cP 25.8 cPRaw Oil from Tanker Truck to Feedstock Tank (T-711), Specific Heat, P-722 2.076 kJ/kg.ºC 0.496 Btu/lb.ºFRaw Oil from Tanker Truck to Feedstock Tank (T-711), Thermal Conductivity, P-722 0.166 W/m.ºC 0.096 Btu/hour.Ft.ºF

Feedstock Tank Heaters (HV-741)Feedstock Tank (T-711), Volume 112,048 Liters 29,600 GallonsFeedstock Storaget High Level percentage at high temperature 95 % 95 %Raw Oil in Feedstock Tank (T-711), Volume 106,446 Liters 28,120 GallonsRaw Oil in Feedstock Tank (T-711), Mass 96,520 kg 212,791 LbsRaw Oil in Feedstock Tank (T-711), Initial Temperature 40 ºC 104 ºFRaw Oil in Feedstock Tank (T-711), Density @ Initial Temperature 0.908 Kg/Liter 7.580 Lbs/GalRaw Oil in Feedstock Tank (T-711), Specific Heat @ Initial Temperature 2.076 kJ/kg.ºC 0.496 Btu/lb.ºFRaw Oil in Feedstock Tank (T-711), Final Temperature 43.5 ºC 110 ºFRaw Oil in Feedstock Tank (T-711), Density @ Final Temperature 0.907 Kg/Liter 7.567 Lbs/GalRaw Oil in Feedstock Tank (T-711), Specific Heat @ Final Temperature 2.086 kJ/kg.ºC 0.499 Btu/lb.ºFEnergy Change 703 MJ 0.67 MMBTUHeat Time 360 Minutes 360 MinutesHeat Load of Feedstock Tank Heaters (HV-741) 33 kW 0.111 MMBTU/hour

Dalhousie Biodiesel PlantDalhousie, New Brunswick, Canada

Process Design Criteria

Items

E3 Energy Partners, LLCSeattle, WA

Metric Unit English Unit

Page 2 of 23




ItemsMetric Unit English Unit

Methanol ReceivingMethanol from Tanker Truck to Methanol Tank (T-511), Voluemtric Flow, P-520 757 LPM 200 GPMMethanol from Tanker Truck to Methanol Tank (T-511), Mass Flow, P-520 600 Kg/Min 1,322 Lbs/MinMethanol from Tanker Truck to Methanol Tank (T-511), Temperature 25 ºC 77 ºFMethanol from Tanker Truck to Methanol Tank (T-511), Process Pressure 1.0 atm 14.7 PsiaMethanol from Tanker Truck to Methanol Tank (T-511), Density 0.792 Kg/Liter 6.611 Lbs/GalMethanol from Tanker Truck to Methanol Tank (T-511), Viscosity 0.6 cP 0.6 cPMethanol from Tanker Truck to Methanol Tank (T-511), Specific Heat 2.542 kJ/kg.ºC 0.607 Btu/lb.ºFMethanol from Tanker Truck to Methanol Tank (T-511), Thermal Conductivity 0.201 W/m.ºC 0.116 Btu/hour.Ft.ºF

Feedstock FilteringRaw Oil from Feedstock Tank (T-711) to Feedstock Final Filter (F-760), Volume 100,000 Liters 26,417 GallonsRaw Oil from Feedstock Tank (T-711) to Feedstock Final Filter (F-760), Mass 90,825 kg 200,236 LbsRaw Oil from Feedstock Tank (T-711) to Feedstock Final Filter (F-760), Transfer Time 20 Minutes 20 MinutesRaw Oil from Feedstock Tank (T-711) to Feedstock Final Filter (F-760), Volumetric Flow, P-720 5,000 LPM 1,321 GPMRaw Oil from Feedstock Tank (T-711) to Feedstock Final Filter (F-760), Mass Flow, P-720 4,541 Kg/Min 10,012 Lbs/MinRaw Oil from Feedstock Tank (T-711) to Feedstock Final Filter (F-760), Temperature 40 ºC 104 ºFRaw Oil from Feedstock Tank (T-711) to Feedstock Final Filter (F-760), Density 0.908 Kg/Liter 7.580 Lbs/GalRaw Oil from Feedstock Tank (T-711) to Feedstock Final Filter (F-760), Viscosity 25.8 cP 25.8 cPRaw Oil from Feedstock Tank (T-711) to Feedstock Final Filter (F-760), Specific Heat 2.076 kJ/kg.ºC 0.496 Btu/lb.ºFRaw Oil from Feedstock Tank (T-711) to Feedstock Final Filter (F-760), Thermal Conductivity 0.166 W/m.ºC 0.096 Btu/hour.Ft.ºF

Raw Oil from Feedstock Final Filter (F-760), Volume 99,550 Liters 26,298 GallonsRaw Oil from Feedstock Final Filter (F-760), Mass 90,417 kg 199,335 LbsRaw Oil from Feedstock Final Filter (F-760), Transfer Time 20 Minutes 20 MinutesRaw Oil from Feedstock Final Filter (F-760), Volumetric Flow 4,978 LPM 1,315 GPMRaw Oil from Feedstock Final Filter (F-760), Mass Flow 4,521 Kg/Min 9,967 Lbs/MinRaw Oil from Feedstock Final Filter (F-760), Temperature 40 ºC 104 ºFRaw Oil from Feedstock Final Filter (F-760), Density 0.908 Kg/Liter 7.580 Lbs/GalRaw Oil from Feedstock Final Filter (F-760), Viscosity 25.8 cP 25.8 cPRaw Oil from Feedstock Final Filter (F-760), Specific Heat 2.076 kJ/kg.ºC 0.496 Btu/lb.ºFRaw Oil from Feedstock Final Filter (F-760), Thermal Conductivity 0.166 W/m.ºC 0.096 Btu/hour.Ft.ºF

Feedstock DryingFeedstock Drying Temperature 80 ºC 176 ºFFeedstock Drying Pressure 0.099 Atm 1.450 PsiaFeedstock Drying Time 300 Minutes 300 Minutes

Page 3 of 23





Raw Oil from Feedstock Final Filter (F-760) to Feedstock Dryer (T-110), Volume per batch 99,550 Liters 26,298 GallonsRaw Oil from Feedstock Final Filter (F-760) to Feedstock Dryer (T-110), Mass per batch 90,417 kg 199,335 LbsRaw Oil from Feedstock Final Filter (F-760) to Feedstock Dryer (T-110), Transfer Time 20 Minutes 20 MinutesRaw Oil from Feedstock Final Filter (F-760) to Feedstock Dryer (T-110), Volumetric Flow 4,978 LPM 1,315 GPMRaw Oil from Feedstock Final Filter (F-760) to Feedstock Dryer (T-110), Mass Flow 4,521 Kg/Min 9,967 Lbs/MinRaw Oil from Feedstock Final Filter (F-760) to Feedstock Dryer (T-110), Temperature 40 ºC 104 ºFRaw Oil from Feedstock Final Filter (F-760) to Feedstock Dryer (T-110), Density 0.908 Kg/Liter 7.580 Lbs/GalRaw Oil from Feedstock Final Filter (F-760) to Feedstock Dryer (T-110), Viscosity 25.8 cP 26 cPRaw Oil from Feedstock Final Filter (F-760) to Feedstock Dryer (T-110), Specific Heat 2.076 kJ/kg.ºC 0.496 Btu/lb.ºFRaw Oil from Feedstock Final Filter (F-760) to Feedstock Dryer (T-110), Thermal Conductivity 0.166 W/m.ºC 0.096 Btu/hour.Ft.ºF

Raw Oil from Feedstock Dryer (T-110) to Biodiesel AE System, Volume 100,619 Liters 26,581 GallonsRaw Oil from Feedstock Dryer (T-110) to Biodiesel AE System, Mass 89,571 kg 197,470 LbsRaw Oil from Feedstock Dryer (T-110) to Biodiesel AE System, Transfer Time 20 Minutes 20 MinutesRaw Oil from Feedstock Dryer (T-110) to Biodiesel AE System, Volumetric Flow, 5,031 LPM 1,329 GPMRaw Oil from Feedstock Dryer (T-110) to Biodiesel AE System, Mass Flow, 4,479 Kg/Min 9,874 Lbs/MinRaw Oil from Feedstock Dryer (T-110) to Biodiesel AE System, Temperature 80 ºC 176 ºFRaw Oil from Feedstock Dryer (T-110) to Biodiesel AE System, Density 0.890 Kg/Liter 7.429 Lbs/GalRaw Oil from Feedstock Dryer (T-110) to Biodiesel AE System, Viscosity 8.4 cP 8.4 cPRaw Oil from Feedstock Dryer (T-110) to Biodiesel AE System, Specific Heat 2.167 kJ/kg.ºC 0.518 Btu/lb.ºFRaw Oil from Feedstock Dryer (T-110) to Biodiesel AE System, Thermal Conductivity 0.158 W/m.ºC 0.092 Btu/hour.Ft.ºF

Water Vapor from Feedstock Dryer (T-110) to Vent, Volume 13,758 cu.M 485,850 cu.FtWater Vapor from Feedstock Dryer (T-110) to Vent, Mass 846 kg 1,865 LbsWater Vapor from Feedstock Dryer (T-110) to Vent, Transfer Time 300 Minutes 300 MinutesWater Vapor from Feedstock Dryer (T-110) to Vent, Volumetric Flow, B-130 2,752 cu.M/Hour 1,620 ACFMWater Vapor from Feedstock Dryer (T-110) to Vent, Mass Flow, B-130 0.17 Kg/Min 6.22 Lbs/MinWater Vapor from Feedstock Dryer (T-110) to Vent, Temperature 80 ºC 176 ºFWater Vapor from Feedstock Dryer (T-110) to Vent, Density 6.15E-05 Kg/Liter 0.004 Lbs/cu.FtWater Vapor from Feedstock Dryer (T-110) to Vent, Viscosity 0.01 cP 0.01 cPWater Vapor from Feedstock Dryer (T-110) to Vent, Specific Heat 1.905 kJ/kg.ºC 0.455 Btu/lb.ºFWater Vapor from Feedstock Dryer (T-110) to Vent, Thermal Conductivity 0.026 W/m.ºC 0.015 Btu/hour.Ft.ºF

Feedstock Dryer Heater (HX-140)Raw Oil in Feedstock Dryer (T-110), Mass 90,417 kg 199,335 LbsRaw Oil in Feedstock Dryer (T-110), Initial Temperature 40 ºC 104 ºFRaw Oil in Feedstock Dryer (T-110), Specific Heat at Initial Temp 2.076 kJ/kg.ºC 0.496 Btu/lb.ºFRaw Oil in Feedstock Dryer (T-110), Final Temperature 80 ºC 176 ºFRaw Oil in Feedstock Dryer (T-110), Specific Heat at Final Temp 2.167 kJ/kg.ºC 0.518 Btu/lb.ºF

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Energy Change for Feedstock Temperature Rising 7,673.07 MJ 7.28 MMBtuWater Vapor, Total Mass 846 kg 1,865 LbsWater Vapor, Heat of Vaporization 2,308 kJ/kg 993 Btu/lbsEnergy Change for Water Evaporation 1,951.99 MJ 1.85 MMBtuEnergy Required, Total 9,625.06 MJ 9.13 MMBtuRaw Oil Drying Time 300 Minutes 300 MinutesHeat Load of Feedstock Dryer Heater (HX-140) 535 kW 1.83 MMBtu/Hour

FullSpectrum ProcessorAcid Esterification Reaction1. LoadingRaw Oil to Biodiesel AE System, Volume 99,550 Liters 26,298 GallonsRaw Oil to Biodiesel AE System, Mass 90,417 kg 199,335 LbsRaw Oil to Biodiesel AE System, Transfer Time 20 Minutes 20 MinutesRaw Oil to Biodiesel AE System, Volumetric Flow, P-722 & P43 4,978 LPM 1,315 GPMRaw Oil to Biodiesel AE System, Mass Flow, P-722 & P43 4,521 Kg/Min 9,967 Lbs/MinRaw Oil to Biodiesel AE System, Temperature 80 ºC 176 ºFRaw Oil to Biodiesel AE System, Density 0.908 Kg/Liter 7.580 Lbs/GalRaw Oil to Biodiesel AE System, Viscosity 25.8 cP 25.8 cPRaw Oil to Biodiesel AE System, Specific Heat 2.167 kJ/kg.ºC 0.518 Btu/lb.ºFRaw Oil to Biodiesel AE System, Thermal Conductivity 0.166 W/m.ºC 0.096 Btu/hour.Ft.ºF

Methanol from Methanol Tank (T-511) to Biodiesel AE System, Volume 11,308 Liters 2,987 GallonsMethanol from Methanol Tank (T-511) to Biodiesel AE System, Mass 8,957 kg 19,747 LbsMethanol from Methanol Tank (T-511) to Biodiesel AE System, Transfer Time 15 Minutes 15 MinutesMethanol from Methanol Tank (T-511) to Biodiesel AE System, Volumetric Flow, P-521 754 LPM 199 GPMMethanol from Methanol Tank (T-511) to Biodiesel AE System, Mass Flow, P-521 12 Kg/Min 1,316 Lbs/MinMethanol from Methanol Tank (T-511) to Biodiesel AE System, Temperature 25 ºC 77 ºFMethanol from Methanol Tank (T-511) to Biodiesel AE System, Density 0.792 Kg/Liter 6.611 Lbs/GalMethanol from Methanol Tank (T-511) to Biodiesel AE System, Viscosity 0.6 cP 0.6 cPMethanol from Methanol Tank (T-511) to Biodiesel AE System, Specific Heat 2.542 kJ/kg.ºC 0.607 Btu/lb.ºFMethanol from Methanol Tank (T-511) to Biodiesel AE System, Thermal Conductivity 0.201 W/m.ºC 0.116 Btu/hour.Ft.ºF

Sulfuric Acid from Sulfuric Acid Tote (T-312) to Biodiesel AE System, Volume 319 Liters 84 GallonsSulfuric Acid from Sulfuric Acid Tote (T-312) to Biodiesel AE System, Mass 582 kg 1,284 LbsSulfuric Acid from Sulfuric Acid Tote (T-312) to Biodiesel AE System, Transfer Time 10 Minutes 10 MinutesSulfuric Acid from Sulfuric Acid Tote (T-312) to Biodiesel AE System, Volumetric Flow, P-322 31.9 LPM 8.4 GPMSulfuric Acid from Sulfuric Acid Tote (T-312) to Biodiesel AE System, Mass Flow, P-322 18 Kg/Min 128 Lbs/MinSulfuric Acid from Sulfuric Acid Tote (T-312) to Biodiesel AE System, Temperature 25 ºC 77 ºF

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Sulfuric Acid from Sulfuric Acid Tote (T-312) to Biodiesel AE System, Density 1.824 Kg/Liter 15.221 Lbs/GalSulfuric Acid from Sulfuric Acid Tote (T-312) to Biodiesel AE System, Viscosity 20.0 cP 20.0 cPSulfuric Acid from Sulfuric Acid Tote (T-312) to Biodiesel AE System, Specific Heat 1.393 kJ/kg.ºC 0.333 Btu/lb.ºFSulfuric Acid from Sulfuric Acid Tote (T-312) to Biodiesel AE System, Thermal Conductivity 0.370 W/m.ºC 0.214 Btu/hour.Ft.ºF

2. ReactionReaction Mixture in Biodiesel AE System after Loading, Total Volume 112,944 Liters 29,837 GallonsReaction Mixture in Biodiesel AE System after Loading, Total Mass 99,110 kg 218,501 LbsReaction Mixture in Biodiesel AE System after Loading, Process Temperature 75 ºC 167 ºFReaction Mixture in Biodiesel AE System after Loading, Density 0.878 Kg/Liter 7.323 Lbs/GalReaction Mixture in Biodiesel AE System after Loading, Viscosity 0.9 cP 0.9 cPReaction Mixture in Biodiesel AE System after Loading, Specific Heat 2.220 kJ/kg.ºC 0.531 Btu/lb.ºFReaction Mixture in Biodiesel AE System after Loading, Thermla Conductivity 0.162 W/m.ºC 0.094 Btu/hour.Ft.ºF

Reaction Mixture in Biodiesel AE System after Reaction, Total Volume 112,971 Liters 29,844 GallonsReaction Mixture in Biodiesel AE System after Reaction, Total Mass 99,110 kg 218,501 LbsReaction Mixture in Biodiesel AE System after Reaction, Temperature 75.0 ºC 167 ºFReaction Mixture in Biodiesel AE System after Reaction, Density 0.877 Kg/Liter 7.322 Lbs/GalReaction Mixture in Biodiesel AE System after Reaction, Viscosity 1.8 cP 1.8 cPReaction Mixture in Biodiesel AE System after Reaction, Specific Heat 2.239 kJ/kg.ºC 0.535 Btu/lb.ºFReaction Mixture in Biodiesel AE System after Reaction, Thermla Conductivity 0.160 W/m.ºC 0.093 Btu/hour.Ft.ºF

3. DrainingGlycerin Phase from Biodiesel AE System to Methanol Flash Recovery, Total Volume 7,818 Liters 2,065 GallonsGlycerin Phase from Biodiesel AE System to Methanol Flash Recovery, Total Mass 7,364 kg 16,236 LbsGlycerin Phase from Biodiesel AE System to Methanol Flash Recovery, Transfer Time 10 Minutes 10 MinutesGlycerin Phase from Biodiesel AE System to Methanol Flash Recovery, Volumetric Flow, P43 782 LPM 207 GPMGlycerin Phase from Biodiesel AE System to Methanol Flash Recovery, Mass Flow, P43 9 Kg/Min 1,624 Lbs/MinGlycerin Phase from Biodiesel AE System to Methanol Flash Recovery, Temperature 75 ºC 167 ºFGlycerin Phase from Biodiesel AE System to Methanol Flash Recovery, Density 0.942 Kg/Liter 7.862 Lbs/GalGlycerin Phase from Biodiesel AE System to Methanol Flash Recovery, Viscosity 1.5 cP 1.5 cPGlycerin Phase from Biodiesel AE System to Methanol Flash Recovery, Specific Heat 2.724 kJ/kg.ºC 0.651 Btu/lb.ºFGlycerin Phase from Biodiesel AE System to Methanol Flash Recovery, Thermal Conductivity 0.239 W/m.ºC 0.138 Btu/hour.Ft.ºF

1st Step Transesterification Reaction1. LoadingOil Phase Remaining in Biodiesel AE System, Total Volume 105,150 Liters 27,778 GallonsOil Phase Remaining in Biodiesel AE System, Total Mass 91,746 kg 202,265 LbsOil Phase Remaining in Biodiesel AE System, Temperature 75 ºC 167 ºF

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Oil Phase Remaining in Biodiesel AE System, Density 0.873 Kg/Liter 7.282 Lbs/GalOil Phase Remaining in Biodiesel AE System, Viscosity 1.9 cP 1.9 cPOil Phase Remaining in Biodiesel AE System, Specific Heat 2.206 kJ/kg.ºC 0.527 Btu/lb.ºFOil Phase Remaining in Biodiesel AE System, Thermal Conductivity 0.157 W/m.ºC 0.091 Btu/hour.Ft.ºF

Methanol from Methanol Tank (T-511) to Biodiesel AE System, Volume 8,437 Liters 2,229 GallonsMethanol from Methanol Tank (T-511) to Biodiesel AE System, Mass 6,683 kg 14,734 LbsMethanol from Methanol Tank (T-511) to Biodiesel AE System, Transfer Time 10 Minutes 10 MinutesMethanol from Methanol Tank (T-511) to Biodiesel AE System, Volumetric Flow, P-521 844 LPM 223 GPMMethanol from Methanol Tank (T-511) to Biodiesel AE System, Mass Flow, P-521 8 Kg/Min 1,473 Lbs/MinMethanol from Methanol Tank (T-511) to Biodiesel AE System, Temperature 25 ºC 77 ºFMethanol from Methanol Tank (T-511) to Biodiesel AE System, Density 0.792 Kg/Liter 6.611 Lbs/GalMethanol from Methanol Tank (T-511) to Biodiesel AE System, Viscosity 0.6 cP 0.6 cPMethanol from Methanol Tank (T-511) to Biodiesel AE System, Specific Heat 2.542 kJ/kg.ºC 0.607 Btu/lb.ºFMethanol from Methanol Tank (T-511) to Biodiesel AE System, Thermal Conductivity 0.201 W/m.ºC 0.116 Btu/hour.Ft.ºF

Methylate from Methylate Tote (T-512) to Biodiesel AE System, Volume 1,214 Liters 321 GallonsMethylate from Methylate Tote (T-512) to Biodiesel AE System, Mass 1,147 kg 2,529 LbsMethylate from Methylate Tote (T-512) to Biodiesel AE System, Transfer Time 15 Minutes 15 MinutesMethylate from Methylate Tote (T-512) to Biodiesel AE System, Volumetric Flow, P-522 81 LPM 21 GPMMethylate from Methylate Tote (T-512) to Biodiesel AE System, Mass Flow, P-522 14 Kg/Min 169 Lbs/MinMethylate from Methylate Tote (T-512) to Biodiesel AE System, Temperature 25 ºC 77 ºFMethylate from Methylate Tote (T-512) to Biodiesel AE System, Density 0.945 Kg/Liter 7.888 Lbs/GalMethylate from Methylate Tote (T-512) to Biodiesel AE System, Viscosity 0.6 cP 0.6 cPMethylate from Methylate Tote (T-512) to Biodiesel AE System, Specific Heat 2.159 kJ/kg.ºC 0.516 Btu/lb.ºFMethylate from Methylate Tote (T-512) to Biodiesel AE System, Thermal Conductivity 0.201 W/m.ºC 0.116 Btu/hour.Ft.ºF

2. ReactionReaction Mixture in Biodiesel AE System after Loading, Total Volume 115,235 Liters 30,442 GallonsReaction Mixture in Biodiesel AE System after Loading, Total Mass 99,576 kg 219,529 LbsReaction Mixture in Biodiesel AE System after Loading, Temperature 70.6 ºC 159 ºFReaction Mixture in Biodiesel AE System after Loading, Density 0.864 Kg/Liter 7.211 Lbs/GalReaction Mixture in Biodiesel AE System after Loading, Viscosity 0.9 cP 0.9 cPReaction Mixture in Biodiesel AE System after Loading, Specific Heat 2.240 kJ/kg.ºC 0.535 Btu/lb.ºFReaction Mixture in Biodiesel AE System after Loading, Thermal Conductivity 0.160 W/m.ºC 0.093 Btu/hour.Ft.ºF

Reaction Mixture in Biodiesel AE System after Reaction, Total Volume 115,726 Liters 30,572 GallonsReaction Mixture in Biodiesel AE System after Reaction, Total Mass 99,576 kg 219,529 LbsReaction Mixture in Biodiesel AE System after Reaction, Temperature 75.0 ºC 167 ºF

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Reaction Mixture in Biodiesel AE System after Reaction, Density 0.860 Kg/Liter 7.181 Lbs/GalReaction Mixture in Biodiesel AE System after Reaction, Viscosity 1.4 cP 1.4 cPReaction Mixture in Biodiesel AE System after Reaction, Specific Heat 2.263 kJ/kg.ºC 0.541 Btu/lb.ºFReaction Mixture in Biodiesel AE System after Reaction, Thermal Conductivity 0.157 W/m.ºC 0.091 Btu/hour.Ft.ºF

3. Transfer to Biodiesel Decanter K3.5 (T-211 )Reaction Mixture from Biodiesel AE System to Settler (T-211), Total Mass 115,726 Liters 30,572 GallonsReaction Mixture from Biodiesel AE System to Settler (T-211), Total Volume 99,576 kg 219,529 LbsReaction Mixture from Biodiesel AE System to Settler (T-211), Transfer Time 20 Minutes 20 MinutesReaction Mixture from Biodiesel AE System to Settler (T-211), Volumetric Flow, P43 5,786 LPM 1,529 GPMReaction Mixture from Biodiesel AE System to Settler (T-211), Mass Flow, P43 4,979 Kg/Min 10,976 Lbs/MinReaction Mixture from Biodiesel AE System to Settler (T-211), Temperature 75.0 ºC 167 ºFReaction Mixture from Biodiesel AE System to Settler (T-211), Density 0.860 Kg/Liter 7.181 Lbs/GalReaction Mixture from Biodiesel AE System to Settler (T-211), Viscosity 1.4 cP 1.4 cPReaction Mixture from Biodiesel AE System to Settler (T-211), Specific Heat 2.263 kJ/kg.ºC 0.541 Btu/lb.ºFReaction Mixture from Biodiesel AE System to Settler (T-211), Thermal Conductivity 0.157 W/m.ºC 0.091 Btu/hour.Ft.ºF

4. DrainingGlycerin Phase from Processor Settler (T-211) to Methanol Flash Recovery (SX-202), Total Volume 7,921 Liters 2,093 GallonsGlycerin Phase from Processor Settler (T-211) to Methanol Flash Recovery (SX-202), Total Mass 7,727 kg 17,035 LbsGlycerin Phase from Processor Settler (T-211) to Methanol Flash Recovery (SX-202), Transfer Time 30 Minutes 30 MinutesGlycerin Phase from Processor Settler (T-211) to Methanol Flash Recovery (SX-202), Volumetric Flow, P-223 264 LPM 70 GPMGlycerin Phase from Processor Settler (T-211) to Methanol Flash Recovery (SX-202), Mass Flow, P-223 29 Kg/Min 568 Lbs/MinGlycerin Phase from Processor Settler (T-211) to Methanol Flash Recovery (SX-202), Temperature 60 ºC 140 ºFGlycerin Phase from Processor Settler (T-211) to Methanol Flash Recovery (SX-202), Density 0.975 Kg/Liter 8.140 Lbs/GalGlycerin Phase from Processor Settler (T-211) to Methanol Flash Recovery (SX-202), Viscosity 2.3 cP 2.3 cPGlycerin Phase from Processor Settler (T-211) to Methanol Flash Recovery (SX-202), Specific Heat 2.568 kJ/kg.ºC 0.614 Btu/lb.ºFGlycerin Phase from Processor Settler (T-211) to Methanol Flash Recovery (SX-202), Thermal Conductivity 0.232 W/m.ºC 0.134 Btu/hour.Ft.ºF

2nd Step Transesterification Reaction1. LoadingOil Phase from Settler (T-211) to Transesterification, Total Volume 106,509 Liters 28,137 GallonsOil Phase from Settler (T-211) to Transesterification, Total Mass 91,850 kg 202,494 LbsOil Phase from Settler (T-211) to Transesterification, Transfer Time 20 Minutes 20 MinutesOil Phase from Settler (T-211) to Transesterification, Volumetric Flow, P-222 5,325 LPM 1,407 GPMOil Phase from Settler (T-211) to Transesterification, Mass Flow, P-222 17 Kg/Min 10,125 Lbs/MinOil Phase from Settler (T-211) to Transesterification, Temperature 60.0 ºC 140 ºFOil Phase from Settler (T-211) to Transesterification, Density 0.862 Kg/Liter 7.197 Lbs/GalOil Phase from Settler (T-211) to Transesterification, Viscosity 1.8 cP 1.8 cP

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Oil Phase from Settler (T-211) to Transesterification, Specific Heat 2.186 kJ/kg.ºC 0.522 Btu/lb.ºFOil Phase from Settler (T-211) to Transesterification, Thermal Conductivity 0.156 W/m.ºC 0.090 Btu/hour.Ft.ºF

Methanol from Methanol Tank (T-511) to Transesterification, Volume 2,812 Liters 743 GallonsMethanol from Methanol Tank (T-511) to Transesterification, Mass 2,228 kg 4,911 LbsMethanol from Methanol Tank (T-511) to Transesterification, Transfer Time 5 Minutes 5 MinutesMethanol from Methanol Tank (T-511) to Transesterification, Volumetric Flow, P-521 562 LPM 149 GPMMethanol from Methanol Tank (T-511) to Transesterification, Mass Flow, P-521 4 Kg/Min 982 Lbs/MinMethanol from Methanol Tank (T-511) to Transesterification, Temperature 25 ºC 77 ºFMethanol from Methanol Tank (T-511) to Transesterification, Density 0.792 Kg/Liter 6.611 Lbs/GalMethanol from Methanol Tank (T-511) to Transesterification, Viscosity 0.6 cP 0.6 cPMethanol from Methanol Tank (T-511) to Transesterification, Specific Heat 2.542 kJ/kg.ºC 0.607 Btu/lb.ºFMethanol from Methanol Tank (T-511) to Transesterification, Thermal Conductivity 0.201 W/m.ºC 0.116 Btu/hour.Ft.ºF

Methylate from Methylate Tote (T-512) to Transesterification, Volume 405 Liters 107 GallonsMethylate from Methylate Tote (T-512) to Transesterification, Mass 382 kg 843 LbsMethylate from Methylate Tote (T-512) to Transesterification, Transfer Time 5 Minutes 5 MinutesMethylate from Methylate Tote (T-512) to Transesterification, Volumetric Flow, P-522 81 LPM 21 GPMMethylate from Methylate Tote (T-512) to Transesterification, Mass Flow, P-522 5 Kg/Min 169 Lbs/MinMethylate from Methylate Tote (T-512) to Transesterification, Temperature 25 ºC 77 ºFMethylate from Methylate Tote (T-512) to Transesterification, Density 0.945 Kg/Liter 7.888 Lbs/GalMethylate from Methylate Tote (T-512) to Transesterification, Viscosity 0.6 cP 0.6 cPMethylate from Methylate Tote (T-512) to Transesterification, Specific Heat 2.159 kJ/kg.ºC 0.516 Btu/lb.ºFMethylate from Methylate Tote (T-512) to Transesterification, Thermal Conductivity 0.201 W/m.ºC 0.116 Btu/hour.Ft.ºF

2. ReactionReaction Mixture in Transesterification after Loading, Total Volume 109,899 Liters 29,032 GallonsReaction Mixture in Transesterification after Loading, Total Mass 94,460 kg 208,248 LbsReaction Mixture in Transesterification after Loading, Temperature 60 ºC 140 ºFReaction Mixture in Transesterification after Loading, Density 0.860 Kg/Liter 7.173 Lbs/GalReaction Mixture in Transesterification after Loading, Viscosity 1.4 cP 1.4 cPReaction Mixture in Transesterification after Loading, Specific Heat 2.201 kJ/kg.ºC 0.526 Btu/lb.ºFReaction Mixture in Transesterification after Loading, Thermla Conductivity 0.157 W/m.ºC 0.091 Btu/hour.Ft.ºF

Reaction Mixture in Transesterification after Reaction, Total Volume 110,584 Liters 29,213 GallonsReaction Mixture in Transesterification after Reaction, Total Mass 94,460 kg 208,248 LbsReaction Mixture in Transesterification after Reaction, Temperature 68 ºC 154 ºFReaction Mixture in Transesterification after Reaction, Density 0.854 Kg/Liter 7.129 Lbs/GalReaction Mixture in Transesterification after Reaction, Viscosity 1.4 cP 1.4 cP

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Reaction Mixture in Transesterification after Reaction, Specific Heat 2.229 kJ/kg.ºC 0.533 Btu/lb.ºFReaction Mixture in Transesterification after Reaction, Thermla Conductivity 0.155 W/m.ºC 0.089 Btu/hour.Ft.ºF

3. Static Methanol EvaporationReaction Mixture in Transesterification after Reaction, Total Volume 109,915 Liters 29,036 GallonsReaction Mixture in Transesterification after Reaction, Total Mass 94,460 kg 208,248 LbsReaction Mixture in Transesterification after Reaction, Temperature 60 ºC 140 ºFReaction Mixture in Transesterification after Reaction, Density 0.859 Kg/Liter 7.172 Lbs/GalReaction Mixture in Transesterification after Reaction, Viscosity 1.6 cP 1.6 cPReaction Mixture in Transesterification after Reaction, Specific Heat 2.203 kJ/kg.ºC 0.527 Btu/lb.ºF

Reaction Mixture in Transesterification after Reaction, Thermla Conductivity 0.156 W/m.ºC 0.090 Btu/hour.Ft.ºFTotal Heat Loss 1,681.70 MJ 1.60 MMBtu

Methanol Heat of Vaporization 1,111 kJ/kg 478 Btu/lbsWater Heat of Vaporization 2,361 kJ/kg 1,016 Btu/lbsGlycerin Heat of Vaporization 1,084 kJ/kg 466 Btu/lbsTotal Heat kJ

Methanol Vapor, Mass 1,478 kg 3,259 LbsMethanol Vapor, Volume 13,003 cu.M 459,190 cu.FtMethanol Vapor, Process Pressure 0.10 Atm 1 PsiaMethanol Vapor, Temperature 60 ºC 140 ºFMethanol Vapor, Static Evaporationi Time 300 Minutes 300 MinutesMethanol Vapor, Volumetric Flow 2,601 cu.M/Hour 1,531 ACFMMethanol Vapor, Mass Flow 296 kg/Hour 652 Lbs/HourMethanol Vapor, Density 0.00 kg/Liter 0.007 Lbs/Cu.ftMethanol Vapor, Specific Heat 1.466 kJ/kg.ºC 0.350 Btu/lb.ºF

Methanol Condensate from Condenser to Recovered Methanol Tank (T-510), Temperature 4 ºC 39 ºFMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Volume 1,802 Liters 476 GallonsMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Density 0.820 Kg/Liter 6.847 Lbs/GalMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Viscosity 0.8 cP 0.8 cPMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Specific Heat 2.489 kJ/kg.ºC 0.595 Btu/lb.ºFMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Thermal Conductivity 0.214 W/m.ºC 0.124 Btu/hour.Ft.ºFMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Volumetric Flow, P-523 6.0 LPM 1.6 GPMMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Mass Flow, P-523 4.9 kg/Min 10.9 Lbs/Min

Reaction Mixture Remaining in Transesterification, Total Volume 107,962 Liters 28,521 GallonsReaction Mixture Remaining in Transesterification, Total Mass 92,982 kg 204,989 Lbs

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Reaction Mixture Remaining in Transesterification, Total Temperature 60.0 ºC 140 ºFReaction Mixture Remaining in Transesterification, Total Density 0.861 Kg/Liter 7.187 Lbs/GalReaction Mixture Remaining in Transesterification, Total Viscosity 1.9 cP 1.9 cPReaction Mixture Remaining in Transesterification, Total Specific Heat 2.193 kJ/kg.ºC 0.524 Btu/lb.ºFReaction Mixture Remaining in Transesterification, Total Thermal Conductivity 0.156 W/m.ºC 0.090 Btu/hour.Ft.ºF

4. DrainingGlycerin Phase from Transesterification to Methanol Flash Recovery (SX-202), Total Volume 2,370 Liters 626 GallonsGlycerin Phase from Transesterification to Methanol Flash Recovery (SX-202), Total Mass 2,307 kg 5,086 LbsGlycerin Phase from Transesterification to Methanol Flash Recovery (SX-202), Transfer Time 10 Minutes 10 MinutesGlycerin Phase from Transesterification to Methanol Flash Recovery (SX-202), Volumetric Flow, TY2 237 LPM 63 GPMGlycerin Phase from Transesterification to Methanol Flash Recovery (SX-202), Mass Flow, TY2 10 Kg/Min 509 Lbs/MinGlycerin Phase from Transesterification to Methanol Flash Recovery (SX-202), Temperature 60 ºC 140 ºFGlycerin Phase from Transesterification to Methanol Flash Recovery (SX-202), Density 0.973 Kg/Liter 8.123 Lbs/GalGlycerin Phase from Transesterification to Methanol Flash Recovery (SX-202), Viscosity 2.7 cP 2.7 cPGlycerin Phase from Transesterification to Methanol Flash Recovery (SX-202), Specific Heat 2.478 kJ/kg.ºC 0.592 Btu/lb.ºFGlycerin Phase from Transesterification to Methanol Flash Recovery (SX-202), Thermal Conductivity 0.215 W/m.ºC 0.125 Btu/hour.Ft.ºF

Biodiesel Phase in Transesterification, Total Volume 105,591 Liters 27,894 GallonsBiodiesel Phase in Transesterification, Total Mass 90,675 kg 199,903 LbsBiodiesel Phase in Transesterification, Total Temperature 60.0 ºC 140 ºFBiodiesel Phase in Transesterification, Total Density 0.859 Kg/Liter 7.166 Lbs/GalBiodiesel Phase in Transesterification, Total Viscosity 1.8 cP 1.8 cPBiodiesel Phase in Transesterification, Total Specific Heat 2.186 kJ/kg.ºC 0.523 Btu/lb.ºFBiodiesel Phase in Transesterification, Total Thermal Conductivity 0.155 W/m.ºC 0.089 Btu/hour.Ft.ºF

5. Deactivation5.1 Deactivation Agent Make-upDeactivation Agent Tote Volume 1,126 Liters 300 GallonsDeactivation Agent Powder (Citric Acid) Per bag per tote 23 kg 50 LbsTotal Batches servered per bag 2.00 Batches 2.00 BatchesTotal Days served Per bag 1.00 Days 1.00 Days

Recovered Methanol from Recovered Methanol Tank (T-510) to Deactivation Agent Tote (T-513), Mass 733 kg 1,617 LbsRecovered Methanol from Recovered Methanol Tank (T-510) to Deactivation Agent Tote (T-513), Volume 909 Liters 240 GallonsRecovered Methanol from Recovered Methanol Tank (T-510) to Deactivation Agent Tote (T-513), Temperature 25 ºC 77 ºFRecovered Methanol from Recovered Methanol Tank (T-510) to Deactivation Agent Tote (T-513), Density 0.807 Kg/Liter 6.735 Lbs/GalRecovered Methanol from Recovered Methanol Tank (T-510) to Deactivation Agent Tote (T-513), Viscosity 0.6 cP 0.6 cPRecovered Methanol from Recovered Methanol Tank (T-510) to Deactivation Agent Tote (T-513), Specific Heat 2.677 kJ/kg.ºC 0.640 Btu/lb.ºF

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Recovered Methanol from Recovered Methanol Tank (T-510) to Deactivation Agent Tote (T-513), Thermal Conductivity 0.216 W/m.ºC 0.125 Btu/hour.Ft.ºFRecovered Methanol from Recovered Methanol Tank (T-510) to Deactivation Agent Tote (T-513), Filling Time 60 Minutes 60 MinutesRecovered Methanol from Recovered Methanol Tank (T-510) to Deactivation Agent Tote (T-513), Volumetric Flow, P-524 12.2 kg/min 26.9 Lbs/MinRecovered Methanol from Recovered Methanol Tank (T-510) to Deactivation Agent Tote (T-513), Mass Flow, P-524 15.1 LPM 4.0 GPM

5.2 DeactivationDeactivation Agent from Deactivation Agent Tote (T-513) to Transesterification, Mass 346 kg 762 LbsDeactivation Agent from Deactivation Agent Tote (T-513) to Transesterification, Volume 420 Liters 111 GallonsDeactivation Agent from Deactivation Agent Tote (T-513) to Transesterification, Temperature 25 ºC 77 ºFDeactivation Agent from Deactivation Agent Tote (T-513) to Transesterification, Density 0.822 Kg/Liter 6.857 Lbs/GalDeactivation Agent from Deactivation Agent Tote (T-513) to Transesterification, Viscosity 0.6 cP 0.6 cPDeactivation Agent from Deactivation Agent Tote (T-513) to Transesterification, Specific Heat 2.632 kJ/kg.ºC 0.629 Btu/lb.ºFDeactivation Agent from Deactivation Agent Tote (T-513) to Transesterification, Thermal Conductivity 0.216 W/m.ºC 0.125 Btu/hour.Ft.ºFDeactivation Agent from Deactivation Agent Tote (T-513) to Transesterification, Transfer Time 5 Minutes 5 MinutesDeactivation Agent from Deactivation Agent Tote (T-513) to Transesterification, Mass Flow, P-525 69.1 kg/min 152.3 Lbs/MinDeactivation Agent from Deactivation Agent Tote (T-513) to Transesterification, Volumetric Flow, P-525 84.1 LPM 22.2 GPM

Biodiesel Phase in Transesterification, Total Volume 106,056 Liters 28,017 GallonsBiodiesel Phase in Transesterification, Total Mass 90,989 kg 200,597 LbsBiodiesel Phase in Transesterification, Total Temperature 60.0 ºC 140 ºFBiodiesel Phase in Transesterification, Total Density 0.858 Kg/Liter 7.160 Lbs/GalBiodiesel Phase in Transesterification, Total Viscosity 1.7 cP 1.7 cPBiodiesel Phase in Transesterification, Total Specific Heat 2.190 kJ/kg.ºC 0.523 Btu/lb.ºFBiodiesel Phase in Transesterification, Total Thermal Conductivity 0.155 W/m.ºC 0.090 Btu/hour.Ft.ºF

6. Dynamic EvaporationBiodiesel Phase in Transesterification, Total Volume 106,056 Liters 28,017 GallonsBiodiesel Phase in Transesterification, Total Mass 90,989 kg 200,597 LbsBiodiesel Phase in Transesterification, Temperature 60.0 ºC 140 ºFBiodiesel Phase in Transesterification, Density 0.858 Kg/Liter 7.160 Lbs/GalBiodiesel Phase in Transesterification, Viscosity 1.7 cP 1.7 cPBiodiesel Phase in Transesterification, Specific Heat 2.190 kJ/kg.ºC 0.523 Btu/lb.ºFBiodiesel Phase in Transesterification, Thermal Conductivity 0.155 W/m.ºC 0.090 Btu/hour.Ft.ºF

Methanol Vapor from Transesterification to Condenser, Volume 29,658 cu.M 1,047,363 cu.FtMethanol Vapor from Transesterification to Condenser, Mass 3,180 kg 7,012 LbsMethanol Vapor from Transesterification to Condenser, Vaporization Time 180 Minutes 180 MinutesMethanol Vapor from Transesterification to Condenser, Temperature 80 ºC 176 ºFMethanol Vapor from Transesterification to Condenser, Pressure 0.099 Atm 1.45 Psia

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Methanol Vapor from Transesterification to Condenser, Density 0.000107 kg/Liter 0.007 Lbs/cu.FtMethanol Vapor from Transesterification to Condenser, Volumetric Flow 9,886 cu.M/Hour 5,819 ACFMMethanol Vapor from Transesterification to Condenser, Mass Flow 18 kg/min 39 Lbs/min

Methanol Condensate from Condenser to Recovered Methanol Tank (T-510), Temperature 4 ºC 39 ºFMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Volume 3,871 Liters 1,023 GallonsMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Density 0.822 Kg/Liter 6.857 Lbs/GalMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Viscosity 0.8 cP 0.8 cPMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Specific Heat 2.472 kJ/kg.ºC 0.591 Btu/lb.ºFMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Thermal Conductivity 0.213 W/m.ºC 0.123 Btu/hour.Ft.ºFMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Volumetric Flow, P-523 21.5 LPM 5.7 GPMMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Mass Flow, P-523 17.7 kg/min 39.0 Lbs/min

Raw Biodiesel in Transesterification after Methanol Removal, Total Volume 103,316 Liters 27,293 GallonsRaw Biodiesel in Transesterification after Methanol Removal, Total Mass 87,809 kg 193,585 LbsRaw Biodiesel in Transesterification after Methanol Removal, Temperature 80.0 ºC 176 ºFRaw Biodiesel in Transesterification after Methanol Removal, Density 0.850 Kg/Liter 7.093 Lbs/GalRaw Biodiesel in Transesterification after Methanol Removal, Viscosity 1.9 cP 1.9 cPRaw Biodiesel in Transesterification after Methanol Removal, Specific Heat 2.225 kJ/kg.ºC 0.532 Btu/lb.ºFRaw Biodiesel in Transesterification after Methanol Removal, Thermal Conductivity 0.150 W/m.ºC 0.086 Btu/hour.Ft.ºF

Refining & Polishing

1. Loading to Raw Biodiesel Sedimentation Tank (T-212)Raw Biodiesel from Transesterification to Raw Biodiesel Sedimentation Tank (T-212), Total Volume 103,316 Liters 27,293 GallonsRaw Biodiesel from Transesterification to Raw Biodiesel Sedimentation Tank (T-212), Total Mass 87,809 kg 193,585 LbsRaw Biodiesel from Transesterification to Raw Biodiesel Sedimentation Tank (T-212), Transfer Time 90 Minutes 90 MinutesRaw Biodiesel from Transesterification to Raw Biodiesel Sedimentation Tank (T-212), Volumetric Flow, TY2 1,148 LPM 303 GPMRaw Biodiesel from Transesterification to Raw Biodiesel Sedimentation Tank (T-212), Mass Flow, TY2 76 Kg/Min 2,151 Lbs/MinRaw Biodiesel from Transesterification to Raw Biodiesel Sedimentation Tank (T-212), Temperature 80 ºC 176 ºFRaw Biodiesel from Transesterification to Raw Biodiesel Sedimentation Tank (T-212), Density 0.850 Kg/Liter 7.093 Lbs/GalRaw Biodiesel from Transesterification to Raw Biodiesel Sedimentation Tank (T-212), Viscosity 1.9 cP 1.9 cPRaw Biodiesel from Transesterification to Raw Biodiesel Sedimentation Tank (T-212), Specific Heat 2.225 kJ/kg.ºC 0.532 Btu/lb.ºFRaw Biodiesel from Transesterification to Raw Biodiesel Sedimentation Tank (T-212), Thermal Conductivity 0.150 W/m.ºC 0.086 Btu/hour.Ft.ºF

2. From Sedimentation Tank (T-212) to Sedimentation Separator (CF-260)Raw Biodiesel from Raw Biodiesel Sedimentation Tank (T-212) to Sedimentation Separator (On SX-200), Volume 103,316 Liters 27,293 GallonsRaw Biodiesel from Raw Biodiesel Sedimentation Tank (T-212) to Sedimentation Separator (On SX-200), Mass 87,809 kg 193,585 Lbs

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Raw Biodiesel from Raw Biodiesel Sedimentation Tank (T-212) to Sedimentation Separator (On SX-200), Transfer Time 360 Minutes 360 MinutesRaw Biodiesel from Raw Biodiesel Sedimentation Tank (T-212) to Sedimentation Separator (On SX-200), Volumetric Flow, P-224 287 LPM 76 GPMRaw Biodiesel from Raw Biodiesel Sedimentation Tank (T-212) to Sedimentation Separator (On SX-200), Mass Flow, P-224 244 Kg/Min 538 Lbs/MinRaw Biodiesel from Raw Biodiesel Sedimentation Tank (T-212) to Sedimentation Separator (On SX-200), Temperature 80 ºC 176 ºFRaw Biodiesel from Raw Biodiesel Sedimentation Tank (T-212) to Sedimentation Separator (On SX-200), Density 0.850 Kg/Liter 7.093 Lbs/GalRaw Biodiesel from Raw Biodiesel Sedimentation Tank (T-212) to Sedimentation Separator (On SX-200), Viscosity 1.9 cP 1.9 cPRaw Biodiesel from Raw Biodiesel Sedimentation Tank (T-212) to Sedimentation Separator (On SX-200), Specific Heat 2.225 kJ/kg.ºC 0.532 Btu/lb.ºFRaw Biodiesel from Raw Biodiesel Sedimentation Tank (T-212) to Sedimentation Separator (On SX-200), Thermal Conductivity 0.150 W/m.ºC 0.086 Btu/hour.Ft.ºF

Glycerin Phase Genrated in Sedimentation Separator (On SX-200), Volume 591 Liters 156 GallonsGlycerin Phase Genrated in Sedimentation Separator (On SX-200), Mass 671 kg 1,480 LbsGlycerin Phase Genrated in Sedimentation Separator (On SX-200), Temperature 80 ºC 176 ºFGlycerin Phase Genrated in Sedimentation Separator (On SX-200), Density 1.136 Kg/Liter 9.477 Lbs/GalGlycerin Phase Genrated in Sedimentation Separator (On SX-200), Viscosity 32.0 cP 32.0 cPGlycerin Phase Genrated in Sedimentation Separator (On SX-200), Specific Heat 2.540 kJ/kg.ºC 0.607 Btu/lb.ºF

Processing Water Frequency, Time per shot 2 minutes 2 MinutesProcessing Water Mass per shot 1.0 kg 2.2 LbsProcessing Water Total Mass 180 kg 396.8 LbsProcessing Water Total Volume 181 Liters 48 GallonsProcessing Water Temperature 25 ºC 77 ºFProcessing Water Density 0.997 Kg/Liter 8.320 Lbs/GalProcessing Water Viscosity 0.9 cP 0.9 cPProcessing Water Specific Heat 4.182 kJ/kg.ºC 1.000 Btu/lb.ºF

Sludge from Sedimentation Separator (On SX-200) to Glycerin Tank (T-410), per Batch, Total Volume 772 Liters 204 GallonsSludge from Sedimentation Separator (On SX-200) to Glycerin Tank (T-410), per Batch, Total Mass 851 kg 1,877 LbsSludge from Sedimentation Separator (On SX-200) to Glycerin Tank (T-410), Temperature 63 ºC 146 ºFSludge from Sedimentation Separator (On SX-200) to Glycerin Tank (T-410), Density 1.103 Kg/Liter 9.204 Lbs/GalSludge from Sedimentation Separator (On SX-200) to Glycerin Tank (T-410), Viscosity 72.5 cP 72.5 cPSludge from Sedimentation Separator (On SX-200) to Glycerin Tank (T-410), Specific Heat 2.868 kJ/kg.ºC 0.686 Btu/lb.ºFSludge from Sedimentation Separator (On SX-200) to Glycerin Tank (T-410), Volumetric Flow 2.14 LPM 0.6 GPMSludge from Sedimentation Separator (On SX-200) to Glycerin Tank (T-410), Mass Flow 2.4 Kg/Min 5.2 Lbs/Min

Raw Biodiesel from Sedimentation Separator (On SX-200) to Purification System (SX-200), Volume 102,724 Liters 27,137 GallonsRaw Biodiesel from Sedimentation Separator (On SX-200) to Purification System (SX-200), Mass 87,137 kg 192,105 LbsRaw Biodiesel from Sedimentation Separator (On SX-200) to Purification System (SX-200), Transfer Time 360 Minutes 360 MinutesRaw Biodiesel from Sedimentation Separator (On SX-200) to Purification System (SX-200), Volumetric Flow 285 LPM 75 GPMRaw Biodiesel from Sedimentation Separator (On SX-200) to Purification System (SX-200), Mass Flow 242 Kg/Min 534 Lbs/Min

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Raw Biodiesel from Sedimentation Separator (On SX-200) to Purification System (SX-200), Temperature 80 ºC 176 ºFRaw Biodiesel from Sedimentation Separator (On SX-200) to Purification System (SX-200), Density 0.848 Kg/Liter 7.079 Lbs/GalRaw Biodiesel from Sedimentation Separator (On SX-200) to Purification System (SX-200), Viscosity 1.8 cP 1.8 cPRaw Biodiesel from Sedimentation Separator (On SX-200) to Purification System (SX-200), Specific Heat 2.223 kJ/kg.ºC 0.531 Btu/lb.ºFRaw Biodiesel from Sedimentation Separator (On SX-200) to Purification System (SX-200), Thermal Conductivity 0.149 W/m.ºC 0.086 Btu/hour.Ft.ºF

3. RefiningRefining Agent from Refinging Agent Tote (T-313) to Sluge Separator on Processor (SX-200), Volume 441 Liters 117 GallonsRefining Agent from Refinging Agent Tote (T-313) to Sluge Separator on Processor (SX-200), Mass 537 kg 1,185 LbsRefining Agent from Refinging Agent Tote (T-313) to Sluge Separator on Processor (SX-200), Transfer Time 360 Minutes 360 MinutesRefining Agent from Refinging Agent Tote (T-313) to Sluge Separator on Processor (SX-200), Volumetric Flow, 73.5 LPH 19.4 GPHRefining Agent from Refinging Agent Tote (T-313) to Sluge Separator on Processor (SX-200), Mass Flow, 438.5 Kg/Hour 11,848.2 Lbs/HourRefining Agent from Refinging Agent Tote (T-313) to Sluge Separator on Processor (SX-200), Temperature 25 ºC 77 ºFRefining Agent from Refinging Agent Tote (T-313) to Sluge Separator on Processor (SX-200), Density 1.218 Kg/Liter 10.165 Lbs/GalRefining Agent from Refinging Agent Tote (T-313) to Sluge Separator on Processor (SX-200), Specific Heat 3.135 kJ/kg.ºC 0.749 Btu/lb.ºF

Sludge from Sluge Separator on Processor (SX-200) to Glycerin Tank (T-410), Mass 524 kg 1,155 LbsSludge from Sluge Separator on Processor (SX-200) to Glycerin Tank (T-410), Transfer Time 360 Minutes 360 MinutesSludge from Sluge Separator on Processor (SX-200) to Glycerin Tank (T-410), Mass flow 1.5 kg/min 3.2 Lbs/MinSludge from Sluge Separator on Processor (SX-200) to Glycerin Tank (T-410), Volumetric Flow 1.5 LPM 0.4 GPMSludge from Sluge Separator on Processor (SX-200) to Glycerin Tank (T-410), Temperature 80 ºC 176 ºF

Biodiesel From Sluge Separator on Process (SX-200) to Purification System (SX-201), Volume 103,204 Liters 27,264 GallonsBiodiesel From Sluge Separator on Process (SX-200) to Purification System (SX-201), Mass 87,592 kg 193,107 LbsBiodiesel From Sluge Separator on Process (SX-200) to Purification System (SX-201), Transfer Time 360 Minutes 360 MinutesBiodiesel From Sluge Separator on Process (SX-200) to Purification System (SX-201), Volumetric Flow 287 LPM 76 GPMBiodiesel From Sluge Separator on Process (SX-200) to Purification System (SX-201), Mass Flow 243 Kg/Min 536 Lbs/MinBiodiesel From Sluge Separator on Process (SX-200) to Purification System (SX-201), Temperature 80 ºC 176 ºFBiodiesel From Sluge Separator on Process (SX-200) to Purification System (SX-201), Density 0.849 Kg/Liter 7.083 Lbs/GalBiodiesel From Sluge Separator on Process (SX-200) to Purification System (SX-201), Viscosity 1.8 cP 1.8 cPBiodiesel From Sluge Separator on Process (SX-200) to Purification System (SX-201), Specific Heat 2.231 kJ/kg.ºC 0.533 Btu/lb.ºFBiodiesel From Sluge Separator on Process (SX-200) to Purification System (SX-201), Thermal Conductivity 0.150 W/m.ºC 0.087 Btu/hour.Ft.ºF

4. Water RemovalBiodiesel from Purification System (SX-201), Volumetric Flow 287 LPM 75.7 GPMBiodiesel from Purification System (SX-201), Mass Flow 243 Kg/Min 536 Lbs/MinBiodiesel from Purification System (SX-201), Temperature 80 ºC 176 ºFBiodiesel from Purification System (SX-201), Density 0.849 Kg/Liter 7.083 Lbs/GalBiodiesel from Purification System (SX-201), Viscosity 1.8 cP 1.8 cP

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Biodiesel from Purification System (SX-201), Specific Heat 2.231 kJ/kg.ºC 0.533 Btu/lb.ºFBiodiesel from Purification System (SX-201), Thermal Conductivity 0.150 W/m.ºC 0.087 Btu/hour.Ft.ºF

Water Vapor from Purification System (SX-201), Volumetric Flow 1,123 cu.M/Hour 661 ACFMWater Vapor from Purification System (SX-201), Mass Flow 82 Kg/Hour 181 Lbs/HourWater Vapor from Purification System (SX-201), Temperature 80 ºC 176 ºFWater Vapor from Purification System (SX-201), Processing Pressure 0.0987 Atm 1.450 PsiaWater Vapor from Purification System (SX-201), Density 0.00 Kg/Liter 4.57E-03 Lbs/cu.FtWater Vapor from Purification System (SX-201), Viscosity 0.01 cP 0.01 cPWater Vapor from Purification System (SX-201), Specific Heat 1.739 kJ/kg.ºC 0.416 Btu/lb.ºFWater Vapor from Purification System (SX-201), Thermal Conductivity 0.023 W/m.ºC 0.013 Btu/hour.Ft.ºF

Water Condensate from water vapor condenser, Volumetric Flow 88.3 LPH 23.3 GPHWater Condensate from water vapor condenser, Mass Flow 82 Kg/Hour 181 Lbs/HourWater Condensate from water vapor condenser, Temperauture 4 ºC 39 ºFWater Condensate from water vapor condenser, Density 0.932 Kg/Liter 7.777 Lbs/cu.FtWater Condensate from water vapor condenser, Viscosity 0.8 cP 0.77 cPWater Condensate from water vapor condenser, Specific Heat 3.548 kJ/kg.ºC 0.848 Btu/lb.ºFWater Condensate from water vapor condenser, Thermal Conductivity 0.375 W/m.ºC 0.217 Btu/hour.Ft.ºF

3. AdditivesBiodiesel from Polishing Separator on Processor (SX-201), Total Volume 102,639 Liters 27,114 GallonsBiodiesel from Polishing Separator on Processor (SX-201), Total Mass 87,098 kg 192,019 LbsBiodiesel from Polishing Separator on Processor (SX-201), Transfer Time 360 Minutes 360 MinutesBiodiesel from Polishing Separator on Processor (SX-201), Volumetric Flow 285.1 LPM 75.3 GPMBiodiesel from Polishing Separator on Processor (SX-201), Mass Flow 241.9 Kg/Min 533.4 Lbs/MinBiodiesel from Polishing Separator on Processor (SX-201), Temperature 80 ºC 176 ºFBiodiesel from Polishing Separator on Processor (SX-201), Density 0.849 Kg/Liter 7.082 Lbs/GalBiodiesel from Polishing Separator on Processor (SX-201), Viscosity 1.9 cP 1.9 cPBiodiesel from Polishing Separator on Processor (SX-201), Specific Heat 2.223 kJ/kg.ºC 0.531 Btu/lb.ºFBiodiesel from Polishing Separator on Processor (SX-201), Thermal Conductivity 0.149 W/m.ºC 0.086 Btu/hour.Ft.ºF

If Antioxidant in one separate Tote only.Pure AntiOxidant Volume Needed for one batch Biodiesel, Volume 102.6 Liters 27.1 GallonsConcentrated Antioxidant/Biodiesel Mixture, Concentration 20.00% V/V 20.00% V/VConcentrated Antioxidant/Biodiesel Mixture, Volume 513.2 Liters 135.6 GallonsBiodiesel Volume needed for Mixing, Volume 410.6 Liters 108.5 Gallons

Concentration Antioxidant/Biodiesel Mixture, Tote Volume 1,135.6 Liters 300.0 Gallons

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Total Biodiesel Needed, Volume 908.5 Liters 240.0 GallonsTotal Antixodant Needed, Volume 227.1 Liters 60.0 GallonsTotal Batches one Tote of Mixed Concentrated Mixture could supply 2.2 Batches 2.2 BatchesConcentrated Antioxidant/Biodiesel Mixture, Feed Flow Rate 85.5 LPH 22.6 GPH

If Winterizing Agent in one separate Tote only.Pure Winterizing Volume Needed for one batch Biodiesel, Volume 513.2 Liters 135.6 GallonsConcentrated Winterizing Agent/Biodiesel Mixture, Concentration 100.00% V/V 100.00% V/VConcentrated Winterizing Agent/Biodiesel Mixture, Volume 513.2 Liters 135.6 GallonsBiodiesel Volume needed for Mixing, Volume 0.0 Liters 0.0 Gallons

Concentration Winterizing Agent/Biodiesel Mixture, Tote Volume 1,135.6 Liters 300.0 GallonsTotal Biodiesel Needed, Volume - Liters - GallonsTotal Winterizing Agent Needed, Volume 1,135.6 Liters 300.0 GallonsTotal Batches one Tote of Mixed Concentrated Mixture could supply 2.2 Batches 2.2 BatchesConcentrated Winterizing Agent /Biodiesel Mixture, Feed Flow Rate 85.5 LPH 22.6 GPH

If Antioxidant and Winterizing Agent prepared in one Tote togetherPure AntiOxidant Volume Needed for one batch Biodiesel, Volume 102.6 Liters 27.1 GallonsPure Winterizing Volume Needed for one batch Biodiesel, Volume 513.2 Liters 135.6 GallonsConcentrated Antioxidant/Biodiesel Mixture, Concentration 10.00% V/V 10.00% V/VConcentrated Winterizing Agent/Biodiesel Mixture, Concentration 50.00% V/V 50.00% V/VConcentrated Additives/Biodiesel Mixture, Volume 1026.4 Liters 271.1 GallonsBiodiesel Volume needed for Mixing, Volume 410.6 Liters 108.5 Gallons

Concentrated Additives/Biodiesel Mixture, Tote Volume 1,135.6 Liters 300.0 GallonsTotal Biodiesel Needed, Volume 454.2 Liters 120.0 GallonsTotal Antioxidant Additive Needed, Volume 113.6 Liters 30.0 GallonsTotal Winterizing Agent Needed, Volume 567.8 Liters 150.0 GallonsTotal Batches one Tote of Mixed Concentrated Mixture could supply 1.1 Batches 1.1 BatchesConcentrated Additives /Biodiesel Mixture, Feed Flow Rate 171.1 LPH 45.2 GPH

4. Biodiesel PolishingBiodiesel from FullSpectrum Processor (SX-201) to Biodiesel Final Filter Skid (SX-600), Volume Flow, 288.0 LPM 76.1 GPMBiodiesel from FullSpectrum Processor (SX-201) to Biodiesel Final Filter Skid (SX-600), Mass Flow, 244.4 Kg/Min 538.7 Lbs/MinBiodiesel from FullSpectrum Processor (SX-201) to Biodiesel Final Filter Skid (SX-600), Temperature 80 ºC 176 ºFBiodiesel from FullSpectrum Processor (SX-201) to Biodiesel Final Filter Skid (SX-600), Density 0.849 Kg/Liter 7.082 Lbs/GalBiodiesel from FullSpectrum Processor (SX-201) to Biodiesel Final Filter Skid (SX-600), Viscosity 1.9 cP 1.9 cPBiodiesel from FullSpectrum Processor (SX-201) to Biodiesel Final Filter Skid (SX-600), Specific Heat 2.223 kJ/kg.ºC 0.531 Btu/lb.ºF

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Biodiesel from FullSpectrum Processor (SX-201) to Biodiesel Final Filter Skid (SX-600), Thermal Conductivity 0.149 W/m.ºC 0.086 Btu/hour.Ft.ºF

Biodiesel from Biodiesel Final Filter Skid (SX-600) to Biodiesel Tank (T-611), Volumetric Flow 288.0 LPM 76.1 GPMBiodiesel from Biodiesel Final Filter Skid (SX-600) to Biodiesel Tank (T-611), Mass Flow 244.4 Kg/Min 538.7 Lbs/MinBiodiesel from Biodiesel Final Filter Skid (SX-600) to Biodiesel Tank (T-611), Temperature 80 ºC 176 ºFBiodiesel from Biodiesel Final Filter Skid (SX-600) to Biodiesel Tank (T-611), Density 0.849 Kg/Liter 7.082 Lbs/GalBiodiesel from Biodiesel Final Filter Skid (SX-600) to Biodiesel Tank (T-611), Viscosity 1.9 cP 1.9 cPBiodiesel from Biodiesel Final Filter Skid (SX-600) to Biodiesel Tank (T-611), Specific Heat 2.223 kJ/kg.ºC 0.531 Btu/lb.ºFBiodiesel from Biodiesel Final Filter Skid (SX-600) to Biodiesel Tank (T-611), Thermal Conductivity 0.149 W/m.ºC 0.086 Btu/hour.Ft.ºF

Biodiesel from Swing Tank (T-610) to Biodiesel Tank (T-611), Volumetric Flow 473.2 LPM 125.0 GPMBiodiesel from Swing Tank (T-610) to Biodiesel Tank (T-611), Mass Flow 401.5 Kg/Min 885.2 Lbs/MinBiodiesel from Swing Tank (T-610) to Biodiesel Tank (T-611), Temperature 80 ºC 176 ºFBiodiesel from Swing Tank (T-610) to Biodiesel Tank (T-611), Density 0.849 Kg/Liter 7.082 Lbs/GalBiodiesel from Swing Tank (T-610) to Biodiesel Tank (T-611), Viscosity 1.9 cP 1.9 cPBiodiesel from Swing Tank (T-610) to Biodiesel Tank (T-611), Specific Heat 2.223 kJ/kg.ºC 0.531 Btu/lb.ºFBiodiesel from Swing Tank (T-610) to Biodiesel Tank (T-611), Thermal Conductivity 0.149 W/m.ºC 0.086 Btu/hour.Ft.ºF

Biodiesel LoadoutBiodiesel Load out from Biodiesel Tank (T-611) , Volumetric Flow, P-622 946.4 LPM 250.0 GPMBiodiesel Load out from Biodiesel Tank (T-611) , Mass Flow, P-622 803.1 Kg/Min 1,770.5 Lbs/MinBiodiesel Load out from Biodiesel Tank (T-611) , Temperature 80 ºC 176 ºFBiodiesel Load out from Biodiesel Tank (T-611) , Density 0.849 Kg/Liter 7.082 Lbs/GalBiodiesel Load out from Biodiesel Tank (T-611) , Viscosity 1.9 cP 1.9 cPBiodiesel Load out from Biodiesel Tank (T-611) , Specific Heat 2.223 kJ/kg.ºC 0.531 Btu/lb.ºFBiodiesel Load out from Biodiesel Tank (T-611) , Thermal Conductivity 0.149 W/m.ºC 0.086 Btu/hour.Ft.ºF

Diesel Blending and Loadout1. Diesel ReceivingPetroleum Diesel from Tanker Truck to (), Volumetric Flow, 946 LPM 250 GPMPetroleum Diesel from Tanker Truck to (), Mass Flow, 804 Kg/Min 1,773 Lbs/MinPetroleum Diesel from Tanker Truck to (), Temperature 25 ºC 77 ºFPetroleum Diesel from Tanker Truck to (), Density 0.850 Kg/Liter 7.094 Lbs/GalPetroleum Diesel from Tanker Truck to (), Viscosity 4.3 cP 4.3 cPPetroleum Diesel from Tanker Truck to (), Specific Heat 2.008 kJ/kg.ºC 0.480 Btu/lb.ºF

2. BlendingBiodiesel Concentration - % V/V - % V/V

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Petroleum Diesel from () to Biodiesel Load-Out Skid (SX-800), Volumetric Flow, 946.4 LPM 250.0 GPMPetroleum Diesel from () to Biodiesel Load-Out Skid (SX-800), Mass Flow, 804.4 Kg/Min 1,773.4 Lbs/MinPetroleum Diesel from () to Biodiesel Load-Out Skid (SX-800), Temperature 25 ºC 77 ºFPetroleum Diesel from () to Biodiesel Load-Out Skid (SX-800), Density 0.850 Kg/Liter 7.094 Lbs/GalPetroleum Diesel from () to Biodiesel Load-Out Skid (SX-800), Viscosity 4.3 cP 4.3 cPPetroleum Diesel from () to Biodiesel Load-Out Skid (SX-800), Specific Heat 2.008 kJ/kg.ºC 0.480 Btu/lb.ºF

Biodiesel from Biodiesel Tank (T-611) to Biodiesel Load-Out Skid (SX-800), Volumetric Flow, P-622 - LPM - GPMBiodiesel from Biodiesel Tank (T-611) to Biodiesel Load-Out Skid (SX-800), Mass Flow, P-622 - Kg/Min - Lbs/MinBiodiesel from Biodiesel Tank (T-611) to Biodiesel Load-Out Skid (SX-800), Temperature 80 ºC 176 ºFBiodiesel from Biodiesel Tank (T-611) to Biodiesel Load-Out Skid (SX-800), Density 0.849 Kg/Liter 7.082 Lbs/GalBiodiesel from Biodiesel Tank (T-611) to Biodiesel Load-Out Skid (SX-800), Viscosity 1.9 cP 1.9 cPBiodiesel from Biodiesel Tank (T-611) to Biodiesel Load-Out Skid (SX-800), Heat Capcity 2.223 kJ/kg.ºC 0.531 Btu/lb.ºF

3. LoadoutBlended Diesel from Biodiesel Load-Out Skid (SX-800), Volumetric Flow 946.4 LPM 250.0 GPMBlended Diesel from Biodiesel Load-Out Skid (SX-800), Mass Flow 804.4 Kg/Min 1,773.4 Lbs/MinBlended Diesel from Biodiesel Load-Out Skid (SX-800), Temperature 25 ºC 77 ºFBlended Diesel from Biodiesel Load-Out Skid (SX-800), Density 0.850 Kg/Liter 7.094 Lbs/GalBlended Diesel from Biodiesel Load-Out Skid (SX-800), Viscosity 2.7 cP 2.7 cPBlended Diesel from Biodiesel Load-Out Skid (SX-800), Specific Heat 2.008 kJ/kg.ºC 0.480 Btu/lb.ºF

Glycerin TreatmentGlycerin Phase from Biodiesel Processors (SX-200, SX-201), Total Volume 18,114 Liters 4,785 GallonsGlycerin Phase from Biodiesel Processors (SX-200, SX-201), Total Mass 17,398 kg 38,356 LbsGlycerin Phase from Biodiesel Processors (SX-200, SX-201), Temperature 66 ºC 151 ºFGlycerin Phase from Biodiesel Processors (SX-200, SX-201), Density 0.960 Kg/Liter 8.015 Lbs/GalGlycerin Phase from Biodiesel Processors (SX-200, SX-201), Viscosity 2.0 cP 2.0 cPGlycerin Phase from Biodiesel Processors (SX-200, SX-201), Specific Heat 2.620 kJ/kg.ºC 0.626 Btu/lb.ºFGlycerin Phase from Biodiesel Processors (SX-200, SX-201), Thermal Conductivity 0.232 W/m.ºC 0.134 Btu/hour.Ft.ºF

Glycerin Treatment Temperature 80 ºC 176 ºFGlycerin Treatment Pressure 0.10 Atm 1.45 PsiaGlycerin Treatment Evaporation Time 210 Minutes 210 Minutes

Methanol Vapor from Methanol Flash Recovery (SX-202) to Biodiesel Processors, Total Volume 55,918 cu.M 1,974,735 cu.FtMethanol Vapor from Methanol Flash Recovery (SX-202) to Biodiesel Processors, Total Mass 5,536 kg 12,204 LbsMethanol Vapor from Methanol Flash Recovery (SX-202) to Biodiesel Processors, Available Treatment Time 210 Minutes 210 MinutesMethanol Vapor from Methanol Flash Recovery (SX-202) to Biodiesel Processors, Temperature 80 ºC 176 ºF

Page 19 of 23





Methanol Vapor from Methanol Flash Recovery (SX-202) to Biodiesel Processors, Processing Pressure 0.099 Atm 1.45 PsiaMethanol Vapor from Methanol Flash Recovery (SX-202) to Biodiesel Processors, Density 0.00 kg/Liter 0.006 Lbs/cu.FtMethanol Vapor from Methanol Flash Recovery (SX-202) to Biodiesel Processors, Volumetric Flow 15,977 cu.M/Hour 9,404 ACFMMethanol Vapor from Methanol Flash Recovery (SX-202) to Biodiesel Processors, Mass Flow 26 kg/min 58 Lbs/min

Methanol Condensate from Condenser to Recovered Methanol Tank (T-510), Temperature 4 ºC 39 ºFMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Volume 6,620 Liters 1,749 GallonsMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Density 0.836 Kg/Liter 6.978 Lbs/GalMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Viscosity 0.8 cP 0.8 cPMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Specific Heat 2.654 kJ/kg.ºC 0.634 Btu/lb.ºFMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Thermal Conductivity 0.230 W/m.ºC 0.133 Btu/hour.Ft.ºFMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Volumetric Flow, P-523 31.5 LPM 8.3 GPMMethanol Condensate from Condenser to Recovered Methanol Tank (T-510), Mass Flow, P-523 26.4 kg/min 58.1 Lbs/min

Glycerin from Methanol Flash Recovery (SX-202) to Glycerin Tank (T-410), Total Volume 10,963 Liters 2,896 GallonsGlycerin from Methanol Flash Recovery (SX-202) to Glycerin Tank (T-410), Total Mass 11,863 kg 26,153 LbsGlycerin from Methanol Flash Recovery (SX-202) to Glycerin Tank (T-410), Transfer Time 30 Minutes 30 MinutesGlycerin from Methanol Flash Recovery (SX-202) to Glycerin Tank (T-410), Volumetric Flow 365 LPM 97 GPMGlycerin from Methanol Flash Recovery (SX-202) to Glycerin Tank (T-410), Mass Flow 395 Kg/Min 872 Lb/MinutesGlycerin from Methanol Flash Recovery (SX-202) to Glycerin Tank (T-410), Temperature 80.0 ºC 176 ºFGlycerin from Methanol Flash Recovery (SX-202) to Glycerin Tank (T-410), Density 1.082 Kg/Liter 9.031 Lbs/GalGlycerin from Methanol Flash Recovery (SX-202) to Glycerin Tank (T-410), Viscosity 19.0 cP 19.0 cPGlycerin from Methanol Flash Recovery (SX-202) to Glycerin Tank (T-410), Specific Heat 2.460 kJ/kg.ºC 0.588 Btu/lb.ºFGlycerin from Methanol Flash Recovery (SX-202) to Glycerin Tank (T-410), Thermal Conductivity 0.251 W/m.ºC 0.145 Btu/hour.Ft.ºF

Glycerin Tank Heater (HV-440)Glycerin Tank (T-410), Volume 56,781 Liters 15,000 GallonsGlycerin Storage, High Level percentage at high temperature 95 % 95 %Glycerin in Glycerin Tank (T-410), Volume 53,942 Liters 14,250 GallonsGlycerin in Glycerin Tank (T-410), Mass 48,360 kg 106,616 LbsGlycerin in Glycerin Tank (T-410), Initial Temperature 60 ºC 140 ºFGlycerin in Glycerin Tank (T-410), Density @ Initial Temperature 0.900 Kg/Liter 7.508 Lbs/GalGlycerin in Glycerin Tank (T-410), Specific Heat @ Initial Temperature 2.378 kJ/kg.ºC 0.568 Btu/lb.ºFGlycerin in Glycerin Tank (T-410), Final Temperature 67 ºC 153 ºFGlycerin in Glycerin Tank (T-410), Density @ Final Temperature 0.897 Kg/Liter 7.482 Lbs/GalGlycerin in Glycerin Tank (T-410), Specific Heat @ Final Temperature 2.406 kJ/kg.ºC 0.575 Btu/lb.ºFEnergy Change 810 MJ 0.77 MMBTUHeat Time 360 Minutes 360 MinutesHeat Load of Glycerin Tank Heater (HV-440) 37 kW 0.128 MMBTU/hour

Page 20 of 23





Hot Water SystemHot Water System, Rated Power 200 kW 0.683 MMBTU/hour

Rated Hot Water Return, Temprature 70 ºC 158 ºFRated Hot Water Return, Density 0.978 Kg/Liter 8.160 Lbs/GalRated Hot Water Return, Viscosity 0.4 cP 0.4 cPRated Hot Water Return, Specific Heat 4.188 kJ/kg.ºC 1.001 Btu/lb.ºFRated Hot Water Return, Thermal Conductivity 0.660 W/m.ºC 0.381 Btu/hour.Ft.ºF

Rated Hot Water Supply Temperature 95 ºC 203 ºFHot Water Supply, Temperature 0.962 Kg/Liter 8.027 Lbs/GalHot Water Supply, Viscosity 0.3 cP 0.3 cPHot Water Supply, Specific Heat 4.211 kJ/kg.ºC 1.006 Btu/lb.ºFHot Water Supply, Thermal Conductivity 0.676 W/m.ºC 0.391 Btu/hour.Ft.ºF

Hot Water to Processor Skids (SX-200, SX-201), Volumetric Flow, P-920, 921 119 LPM 31 GPMHot Water to Processor Skids (SX-200, SX-201), Mass Flow, P-920, 921 114 Kg/Min 252 Lb/Minutes

If using Natural Gas as FuelNatural Gas Heat of Combustion, HHV 38,416.00 kJ/m3 1,031.74 Btu/Cu.ftNatural Gas Heat of Combustion, LHV 34,574.40 kJ/m3 928.57 Btu/Cu.ftHeat Utilization Efficiency 85 % 85 %Natural Gas Average Mass Flow 0.29 kg/min 0.65 lbs/minNatural Gas Average Std. Volumetric Flow 22.05 SCMH 778.68 SCFH

If using Propane as FuelPropane Heat of Combustion, HHV 48.81 MJ/kg 21,000.00 Btu/lbsPropane Heat of Combustion, LHV 46.36 kJ/m3 19,943.26 Btu/lbsHeat Utilization Efficiency 85 % 85 %Propane Average Mass Flow 0.29 kg/min 0.64 lbs/minPropane Average Std. Volumetric Flow 9.20 SCMH 325.04 SCFH

If using Petroleum Diesel as FuelDiesel Heat of Combustion, HHV 44.86 MJ/kg 19,300.00 Btu/lbsDiesel Heat of Combustion, LHV 40.38 kJ/m3 17,370.00 Btu/lbsHeat Utilization Efficiency 85 % 85 %Diesel Average Mass Flow 0.31 kg/min 0.69 lbs/minDiesel Average Std. Volumetric Flow 0.37 LPM 0.10 GPM

Page 21 of 23





If using BioDiesel as FuelBiodiesel Heat of Combustion, HHV 40.29 MJ/kg 17,334.63 Btu/lbsBiodiesel Heat of Combustion, LHV 36.26 kJ/m3 15,601.17 Btu/lbsHeat Utilization Efficiency 85 % 85 %Biodiesel Average Mass Flow 0.35 kg/min 0.77 lbs/minBiodiesel Average Std. Volumetric Flow 0.40 LPM 0.11 GPM

UTILITIES2. NitrogenBatch Usage 16.91 Std. cu.M 597.13 Std. cu. FtBatches a day 0.16603016 Batches 0.16603016 BatchesDaily Usage 2.81 Std. cu.M 99.14158932 Std. cu. Ft

3. Electricity

4. Processing WaterProcess Water for Retention Separator, Frequency shot/min shot/minProcess Water for Retention Separator, Per shot kg/shot lbs/shotProcess Water for Sludge Separator on A, Frequency shot/min shot/minProcess Water for Sludge Separator on A, Per shot kg/shot lbs/shotProcess Water for Sludge Separator on B, Frequency shot/min shot/minProcess Water for Sludge Separator on B, Per shot kg/shot lbs/shotProcess Water for Centrifuge, Total Mass, Daily Kg LbsProcess Water for Centrifuge, Total Volume, Daily Liters Gallons

Hot Water Boiler Capacity, Volume Liters GallonsProcess Water for Hot Water Boiler make-up percentage, per day % %Process Water for Hot Water Boiler make-up, Mass, per day Kg LbsProcess Water for Hot Water Boiler make-up, Volume, per day Liters Gallons

Vacuum Pump Sealing Water Tank, Volume Liters GallonsVacuum Pump Sealing Water Tank Refreshment per day per dayVacuum Pump Sealing Water Tank, Numbers per ProcessorProcess Water for Vacuum Pump Sealing Water Tank refreshment, per day Liters Gallons

Total Processing Water consumption, Daily Liters Gallons

Page 22 of 23





5.SewerVacuum Pump Sealing Water Tank Drain, Volume, Per day Liters GallonsWater Condensate Produced in processors, per batch Liters Gallons

Total Water to swage, Volume per day Liters Gallons

6. Compressed AirAir Flow to Owner's system ACM ACFMAir Pressure Bar PsigDaily Air Consumption, Maximum ACM ACFM

Tanker Truck Traffic Information (Per Week Statistics)1. Feedstock Delivery TruckWeekly Feedstock Consumption, Volume Liters GallonsTanker Truck Volume Liters GallonsTotal Trucks per week Trucks/week Trucks/week

2. Fresh Methanol Delivery TruckRecovered Methanol Reuse Percentage % %Weekly Fresh Methanol Consumption, Volume Liters GallonsTanker Truck Volume Liters GallonsTotal Trucks per week Trucks/week Trucks/week

3. Biodiesel Delivery TruckWeekly Biodiesel Production, Volume Liters GallonsTanker Truck Volume Liters GallonsTotal Trucks per week Trucks/week Trucks/week

4. Glycerin Loadout TruckWeekly Glycerin Production, Volume Liters GallonsWeekly Recovered Methanol Disposal, Volume Liters GallonsWekkly Total Load out, Volume Liters GallonsTanker Truck Volume Liters GallonsTotal Trucks per week Trucks/week Trucks/week

Chemical Totes Refreshment Information (Per Week Statistics)1. Methylate TotesWeekly Methylate Consumption, Volume Liters Gallons

Page 23 of 23





Std IBC Tote Volume Liters GallonsActual Liquid Volume in Tote Liters GallonsTotal Totes per week Totes/week Totes/week

2. Sulfuric Acid TotesWeekly Sulfuric Acid Consumption, Volume Liters GallonsStd IBC Tote Volume Liters GallonsActual Liquid Volume in Tote Liters GallonsTotal Totes per week Totes/week Totes/week

3.Refining Agent TotesWeekly Refining Agent Consumption, Volume Liters GallonsStd IBC Tote Volume Liters GallonsActual Liquid Volume in Tote Liters GallonsTotal Totes per week Totes/week Totes/week

4.Deactivation Agent TotesWeekly Deactivation Agent Consumption, Volume Liters GallonsStd IBC Tote Volume Liters GallonsActual Liquid Volume in Tote Liters GallonsTotal Totes per week Totes/week Totes/week


ATTACHMENT 7.03

Seattle, WA 98104www.e3energypartners.com

Tel: (206) 462-3600Fax: (206) 462-3599


Tel: (206) 462-3600Fax: (206) 462-3599


Tel: (206) 462-3600Fax: (206) 462-3599


Tel: (206) 462-3600Fax: (206) 462-3599


Tel: (206) 462-3600Fax: (206) 462-3599


Tel: (206) 462-3600Fax: (206) 462-3599


ATTACHMENT 7.04

2B Green BioEnergy Corporation Mass/Energy Balance Design Parameters

Page 1 of 3

GeneralFFA, wt% in FeedStock 12.50 %

Operation Days 350.00 Feedstock Batch Process Volume 100,000 Liters

26,417 GallonsFeedstock Batch Process Mass 90,825 kg

Batches a day 2.00 batchesAnnual Process Capacity 18,492,044 Gallons

70,015,231 litersFeedStock

Fresh Raw OilAssuming Refined, Bleached, and Degummed

Moisture 1.00 %wtSolids 0.50 %wt

Unsaponifiable 1.00 %wtPhospholipids 1.00 %wt

total MIU 3.50 %wtFFA 12.50 %TG 84.00 %

Saponification Value 185.22 g KOH/kg oilChemical Composition

H2SO4 acidConcentration 95.00 %wt

Moisture 5.00 %wt

MethanolConcentration 99.50 %wt

Moisture 0.50 %wt

MethylateConcentration 30.00 %wt

Methanol 70.00 %wt


Page 2 of 3

Process DataOverall Filter Effiicency 90.00 %

Raw DryerTemperature 80.00 ºC

Pressure 0.100 Bar2.95 inHg absolute

Acid EsterificationH2SO4 addtion 0.65 wt%

Methanol 10.00 wt%FFA conversion 98.00 %

Overall FAME conversion 50.00 %Reaction Temperature 75.00 ºC

Transesterification reactionOverall Methylate addition 1.00 wt%Methanol : TG molar ratio 6.00

1st setp partition 75.00 %2nd step partition 25.00 %

TG conversion in 1st Step 80.00 %TG conversion in 2nd Step 95.00 %

Overall Conversion 99.00 %

Reaction Temperature 70.00 ºC

Pressure for Dynamic Evaporation 0.10000 BarTemperature for Dynamic Evaporation 80.00 ºC

PurificationRefining Agent Addition Ratio 0.60 wt%

AlCl3 Concentration in solution 30.00 wt%

Water Removel Temperature 80.00 ºC


Page 3 of 3

Water Removal Pressure 0.10000 Bar

Additives Preparation Assuming same density as biodiesAntioxidant to Final B100 Ratio 0.10 % V/V

Winterizing Agent to Finla B100 Ratio 0.50 % V/V

Methanol Flash SystemMRS Temperature 80.00 ºC

MRS Pressure 0.1000 Bar

Deactivation AgentCitric Acid Concentration 3.0 %wt

Recovered Methanol 97.0 %wt

Page 1 of 2

Date March, 2nd, 2010Mass and Energy Balance, Unit: kg

Stream # Material Description From To Biodiesel FFA TG DG MG Glycerol MeOH H2O AlCl3 Al(OH)3 NaOH NaOMe NaFFA C6H8O7Na3C6H5O NaCl H2SO4 Al2(SO4)3 Na2SO4 Phospholipid Unsaponified Solids Total1 Yellow Grease Feedstock Storage Tank FeedStock Filter - 11,353 76,293.4 - - - - 908.3 - - - - - - - - - - - 908.3 908.3 454.1 90,825.5 2 Yellow Grease Feedstock Filter Feedstock Dryer - 11,353 76,293.4 - - - - 908.3 - - - - - - - - - - - 908.3 908.3 45.4 90,416.8 3 Rejected Waste Feedstock Filter Waste - - - - - - - - - - - - - - - - - - - - - 408.7 408.7 4 Water Vapor Feedstock Dryer Ventilation - 0.0 - - - - - 845.7 - - - - - - - - - - - - - - 845.7 5 Yellow Grease Feedstock Dryer Biodiesel Processor AE - ####### 76,293.4 - - - - 62.5 - - - - - - - - - - - 908.3 908.3 45.4 89,571.1 6 Esterificaiton Methanol Methanol Storage Tank Biodiesel Processor AE - - - - - - 8,912.3 44.8 - - - - - - - - - - - - - - 8,957.1 7 Sulfuric acid Sulfuric Acid Tote Biodiesel Processor AE - - - - - - 0.0 29.1 - - - - - - - - 553.1 - - - - - 582.2

Reaction Mixture Biodiesel Processor AE Biodiesel Processor AE - ####### 76,293.4 - - - 8,912.3 136.4 - - - - - - - - 553.1 - - 908.3 908.3 45.4 99,110.4 8 Reaction Mixture at Esterification Reaction End Biodiesel Processor AE Biodiesel Processor AE 43,823.3 227.1 44,298.3 - - 3,345.5 4,151.2 850.0 - - - - - - - - 553.1 - - 908.3 908.3 45.4 99,110.4 9 Glycerin Phase Biodiesel Processor AE Biodiesel Processor MeOH Flash 2.408 0.1 0.0 - - 3,324.7 2,412.2 653.9 - - - - - - - - 524.5 - - 726.6 726.6 45.4 8,416.4

10 Oil Phase Biodiesel Processor AE Biodiesel Processor AE 43,820.9 226.9 44,298.3 - - 20.8 1,739.1 196.1 - - - - - - - - 28.6 - - 181.7 181.7 - 90,694.0 9 Decanted Glycerin Phase Biodiesel Processor AE Biodiesel Processor MeOH Flash 306.9 1.7 308.3 - - 2,659.9 1,941.9 524.4 - - - - - - - - 419.8 - - 582.5 582.5 36.3 7,364.4

10 Oil Phase Biodiesel Processor AE Biodiesel Processor AE 43,516.4 225.4 43,990.0 - - 685.6 2,209.4 325.5 - - - - - - - - 133.3 - - 325.7 325.7 9.1 91,746.0 11 Methanol, 1st Step TransEster. Methanol Storage Tank Biodiesel Processor Trans - - - - - - 6,649.8 33.4 - - - - - - - - - - - - - - 6,683.2 12 Methylate,1st Step TransEster. Methylate Tote Biodiesel Processor Trans - - - - - - 803.1 - - - - 344.2 - - - - - - - - - - 1,147.3

Reaction Mixture Biodiesel Processor Trans Biodiesel Processor Trans 43,516.4 - 43,990.0 - - 685.6 9,775.0 359.0 - - - 154.0 243.0 - - - - - 193.0 325.7 325.7 9.1 99,576.4 13 Reaction Mixture at 1st Trans.Ester. end Biodiesel Processor Trans Biodiesel Processor Settler 78,869.4 - 8,798.0 - - 4,365.3 5,934.2 359.0 - - - 154.0 243.0 - - - - - 193.0 325.7 325.7 9.1 99,576.4 14 Glycerin Phase, Drain Biodiesel Processor MeOH Flash Biodiesel Processor Settler 5.0 - 0.0 - - 4,326.3 2,970.2 243.5 - - - 127.1 218.7 - - - - - 173.5 260.6 260.6 - 8,585.4 15 Oil Phase Biodiesel Processor MeOH Flash Biodiesel Processor Settler 78,864.5 - 8,798.0 - - 39.0 2,964.0 115.4 - - - 26.9 24.3 - - - - - 19.6 65.1 65.1 - 90,982.0 14 Glycerin Phase, Drain Biodiesel Processor MeOH Flash Biodiesel Processor MeOH Flash 376.3 - 41.5 - - 3,677.5 2,538.7 207.6 - - - 108.1 186.0 - - - - - 147.5 221.8 221.8 - 7,726.8 15 Oil Phase Biodiesel Processor MeOH Flash Biodiesel Processor 2nd Trans 78,493.1 - 8,756.5 - - 687.8 3,395.5 151.4 - - - 45.9 57.0 - - - - - 45.5 103.9 103.9 9.1 91,849.6 16 Methanol Methanol Storage Tank Biodiesel Processor 2nd Trans - - - - - - 2,216.6 11.1 - - - - - - - - - - - - - - 2,227.7 17 Methylate Methylate Tote Biodiesel Processor 2nd Trans - - - - - - 267.7 - - - - 114.7 - - - - - - - - - - 382.4

Reaction Mixture Biodiesel Processor 2nd Trans Biodiesel Processor 2nd Trans 78,493.1 - 8,756.5 - - 687.8 5,879.8 162.5 - - - 160.6 57.0 - - - - - 45.5 103.9 103.9 9.1 94,459.8 18 Reaction Mixture at end Biodiesel Processor 2nd Trans Biodiesel Processor 2nd Trans 86,849.8 - 437.8 - - 1,557.6 4,971.9 162.5 - - - 160.6 57.0 - - - - - 45.5 103.9 103.9 9.1 94,459.8 19 Methanol Vapor, Static Biodiesel Processor 2nd Trans Methanol Condenser 0.0 - - - - 0.2 1,418.9 59.0 - - - - - - - - - - - - - - 1,478.1 20 Reaction Mixture after Static Evaporization Biodiesel Processor 2nd Trans Biodiesel Processor 2nd Trans 86,849.8 - 437.8 - - 1,557.4 3,553.0 103.5 - - - 160.6 57.0 - - - - - 45.5 103.9 103.9 9.1 92,981.6 21 Glycerin Phase, Drain Biodiesel Processor 2nd Trans Biodiesel Processor MeOH Flash 417.6 - 2.1 - - 994.1 612.5 28.6 - - - 79.7 33.4 - - - - - 24.9 54.1 54.1 5.9 2,307.0 22 Raw Biodiesel Biodiesel Processor 2nd Trans Biodiesel Processor 2nd Trans 86,432.2 - 435.7 - - 563.3 2,940.6 75.0 - - - 80.9 23.6 - - - - - 20.6 49.8 49.8 3.2 90,674.7 23 Deactivation Agent Deactivation Agent Tote Biodiesel Processor 2nd Trans 0.1 (0.0) - - - 1.1 304.7 29.3 - - - - - 10.4 - - - - - - - - 345.5 24 Raw Biodiesel After Deactivation Biodiesel Processor 2nd Trans Biodiesel Processor 2nd Trans 86,432.3 21.9 435.7 - - 564.4 3,293.2 104.2 - - - - - - 13.9 - - - 20.6 49.8 49.8 3.2 90,989.1 25 Methanol Vapor, Dynamic Biodiesel Processor 2nd Trans Methanol Condenser 2.6 (0.0) - - - 28.6 3,050.2 99.1 - - - - - - - - - - - - - - 3,180.5 26 Raw Biodiesel Biodiesel Processor 2nd Trans Retention Tank then Retention Separator 86,429.7 21.9 435.7 - - 535.8 243.1 5.1 - - - - - - 13.9 - - - 20.6 49.8 49.8 3.2 87,808.6 27 Glycerin Phase Retention Separator Glycerin Tank 43.2 0.0 0.2 - - 509.0 0.1 4.1 - - - 0 - - 13.9 - - - 19.6 39.8 39.8 1.6 671.4 28 Raw Biodiesel Retention Separator Biodiesel Purification 86,386.5 21.9 435.5 - - 26.8 242.9 1.0 - - - - - - - - - - 1.1 10.0 10.0 1.6 87,137.2 29 Refining Agent Refining Agent Tote Sludge Centrifuge - - - - - - - 376.2 161.2 - - - - - - - - - - - - - 537.4

Refining Mixture Biodiesel Processor Purification Biodiesel Purification 86,386.5 21.9 435.5 - - 26.8 242.9 377.2 161.2 - - - - - - - - - 1.1 49.8 49.8 3.2 87,755.9 30 Sludge Sludge Centrifuge Glycerin Tank - - - - - - - - 161.2 - - - - - - - - - - - - 2.9 164.1 31 Biodiesel Sludge Centrifuge Biodiesel Purification 86,386.5 21.9 435.5 - - 26.8 242.9 377.2 - - - - - - - - - - 1.1 49.8 49.8 0.3 87,591.8 32 Water Vapor Biodiesel Purification Water Vapor Condenser 0.6 - - - - 0.4 181.3 311.2 - - - - - - - - - - - - - - 493.5 33 Biodiesel Biodiesel Purification Batch Test Tank 86,385.9 21.9 435.5 - - 26.4 61.7 66.0 - - - - - - - - - - 1.1 49.8 49.8 0.3 87,098.3 34 Glycerin Phase Process Biodiesel Processor MeOH Flash 1,100.8 1.7 351.9 - - 7,331.5 5,093.0 760.6 - - - 187.8 219.4 - - - 419.8 - 172.4 858.5 858.5 42.2 17,398.2 35 Methanol Vapor Biodiesel Processor MeOH Flash Methanol Condenser - - - - - 4.6 4,798.9 732.0 - - - - - - - - - - - - - - 5,535.5 36 Glycerin Biodiesel Processor MeOH Flash Glycerin Tank 1,100.8 1.7 351.9 - - 7,327.0 294.1 28.6 - - - 187.8 219.4 - - - 419.8 - 172.4 858.5 858.5 42.2 11,862.7

- - - - - - - - - - - - - - - - - - - - - - 0.8 0.075

Recovered Methanol Composition 2.6 (0.0) - - - 33.4 9,268.0 890.1 - - - - - - - - - - - 0.85 0.05 10,194 0.65 0.15

43.215 0.011 0.218 - - 508.995 0.122 184.120 - - - - - - 13.923 - - - 19.583 39.825 39.825 1.589

Page 2 of 2

Mass and Energy Balance, Unit: kmolStream # Material Description From To Biodiesel FFA TG DG MG Glycerol MeOH H2O AlCl3 Al(OH)3 NaOH NaOMe NaFFA C6H8O7Na3C6H5O NaCl H2SO4 Al2(SO4)3 Na2SO4 Phospholipid Unsaponified Solids Total

1 Yellow Grease Feedstock Storage Tank FeedStock Filter - 40.416 86.622 - - - - 50.416 - - - - - - - - - - - 177.454 2 Yellow Grease Feedstock Filter Feedstock Dryer - 40.416 86.622 - - - - 50.416 - - - - - - - - - - - 177.454 3 Rejected Waste Feedstock Filter Waste - - - - - - - - - - - - - - - - - - - - 4 Water Vapor Feedstock Dryer Ventilation - 0.000 - - - - - 46.944 - - - - - - - - - - - 46.944 5 Yellow Grease Feedstock Dryer Biodiesel Processor AE - 40.416 86.622 - - - - 3.472 - - - - - - - - - - - 130.510 6 Esterificaiton Methanol Methanol Storage Tank Biodiesel Processor AE - - - - - - 278.144 2.486 - - - - - - - - - - - 280.630 7 Sulfuric acid Sulfuric Acid Tote Biodiesel Processor AE - - - - - - 0.000 1.616 - - - - - - - - 5.639 - - 7.255 0 Reaction Mixture Biodiesel Processor AE Biodiesel Processor AE - 40.416 86.622 - - - 278.144 7.574 - - - - - - - - 5.639 - - 418.395 8 Reaction Mixture at Esterification Reaction End Biodiesel Processor AE Biodiesel Processor AE 148.588 0.808 50.295 - - 36.327 129.556 47.182 - - - - - - - - 5.639 - - 418.395 9 Decanted Glycerin Phase Biodiesel Processor AE Biodiesel Processor MeOH Flash 1.041 0.006 0.350 - - 28.882 60.603 29.111 - - - - - - - - 4.280 - - 124.274

10 Oil Phase Biodiesel Processor AE Biodiesel Processor AE 147.547 0.802 49.945 - - 7.444 68.952 18.071 - - - - - - - - 1.359 - - 294.121 11 Methanol, 1st Step TransEster. Methanol Storage Tank Biodiesel Processor Trans - - - - - - 207.531 1.855 - - - - - - - - - - - 209.386 12 Methylate,1st Step TransEster. Methylate Tote Biodiesel Processor Trans - - - - - - 25.063 - - - - 6.371 - - - - - - - 31.434 0 Reaction Mixture Biodiesel Processor Trans Biodiesel Processor Trans 147.547 - 49.945 - - 7.444 305.068 19.925 - - - 2.850 0.802 - - - - - 1.359 534.942

13 Reaction Mixture at 1st Trans.Ester. end Biodiesel Processor Trans Biodiesel Processor Settler 267.416 - 9.989 - - 47.400 185.199 19.925 - - - 2.850 0.802 - - - - - 1.359 534.942 1.000 1.000 1.000 1.000 1.000

14 Glycerin Phase, Drain Biodiesel Processor MeOH Flash Biodiesel Processor Settler 0.017 - 0.000 - - 46.976 92.696 13.519 - - - 2.352 0.722 - - - - - 1.221 157.504 15 Oil Phase Biodiesel Processor MeOH Flash Biodiesel Processor Settler 267.399 - 9.989 - - 0.424 92.503 6.407 - - - 0.498 0.080 - - - - - 0.138 377.438 14 Glycerin Phase, Drain Biodiesel Processor MeOH Flash Biodiesel Processor MeOH Flash 1.276 - 0.047 - - 39.932 79.228 11.521 - - - 2.001 0.614 - - - - - 1.039 135.659 15 Oil Phase Biodiesel Processor MeOH Flash Biodiesel Processor 2nd Trans 266.140 - 9.942 - - 7.468 105.971 8.404 - - - 0.849 0.188 - - - - - 0.320 399.283 16 Methanol Methanol Storage Tank Biodiesel Processor 2nd Trans - - - - - - 69.177 0.618 - - - - - - - - - - - 69.795 17 Methylate Methylate Tote Biodiesel Processor 2nd Trans - - - - - - 8.354 - - - - 2.124 - - - - - - - 10.478 0 Reaction Mixture Biodiesel Processor 2nd Trans Biodiesel Processor 2nd Trans 266.140 - 9.942 - - 7.468 183.502 9.022 - - - 2.973 0.188 - - - - - 0.320 479.556

18 Reaction Mixture at end Biodiesel Processor 2nd Trans Biodiesel Processor 2nd Trans 294.474 - 0.497 - - 16.913 155.168 9.022 - - - 2.973 0.188 - - - - - 0.320 479.556 19 Methanol Vapor, Static Biodiesel Processor 2nd Trans Methanol Condenser 0.000 - - - - 0.002 44.281 3.275 - - - - - - - - - - - 47.558 20 Reaction Mixture after Static Evaporization Biodiesel Processor 2nd Trans Biodiesel Processor 2nd Trans 294.474 - 0.497 - - 16.911 110.887 5.748 - - - 2.973 0.188 - - - - - 0.320 431.998

1.000 - 1.000 - - 1.000 1.000 1.000 21 Glycerin Phase, Drain Biodiesel Processor 2nd Trans Biodiesel Processor MeOH Flash 0.003 - 0.000 - - 16.604 28.801 2.416 - - - 2.265 0.169 - - - - - 0.269 50.527 22 Oil Phase Biodiesel Processor 2nd Trans Biodiesel Processor 2nd Trans 294.471 - 0.497 - - 0.307 82.086 3.331 - - - 0.708 0.019 - - - - - 0.051 381.470 21 Glycerin Phase, Drain Biodiesel Processor 2nd Trans Biodiesel Processor MeOH Flash 1.416 - 0.002 - - 10.794 19.114 1.587 - - - 1.476 0.110 - - - - - 0.175 34.674 22 Raw Biodiesel Biodiesel Processor 2nd Trans Biodiesel Processor 2nd Trans 293.058 - 0.495 - - 6.117 91.772 4.161 - - - 1.497 0.078 - - - - - 0.145 397.323 23 Deactivation Agent Deactivation Agent Tote Biodiesel Processor 2nd Trans 0.000 (0.000) - - - 0.012 9.509 1.624 - - - - - 0.054 - - - - - 11.199 24 Raw Biodiesel After Deactivation Biodiesel Processor 2nd Trans Biodiesel Processor 2nd Trans 293.059 0.078 0.495 - - 6.129 102.778 5.785 - - - - - - 0.054 - - - 0.145 408.523 25 Methanol Vapor, Dynamic Biodiesel Processor 2nd Trans Methanol Condenser 0.009 (0.000) - - - 0.311 95.193 5.499 - - - - - - - - - - - 101.012 26 Raw Biodiesel Biodiesel Processor 2nd Trans Retention Tank then Retention Separator 293.050 0.078 0.495 - - 5.818 7.585 0.286 - - - - - - 0.054 - - - 0.145 307.511 27 Glycerin Phase Retention Separator Glycerin Tank 0.147 0.000 0.000 - - 5.527 0.004 0.229 - - - - - - 0.054 - - - 0.138 6.098 28 Raw Biodiesel Retention Separator Biodiesel Purification 292.903 0.078 0.494 - - 0.291 7.582 0.057 - - - - - - - - - - 0.007 301.413 29 Refining Agent Refining Agent Tote Sludge Centrifuge - - - - - - - 20.882 0.202 - - - - - - - - - - 21.084 0 Refining Mixture Biodiesel Processor Purification Biodiesel Purification 292.903 0.078 0.494 - - 0.291 7.582 20.939 0.202 - - - - - - - - - 0.007 322.497

30 Sludge Sludge Centrifuge Glycerin Tank - - - - - - - - 0.202 - - - - - - - - - - 0.202 31 Biodiesel Sludge Centrifuge Biodiesel Purification 292.903 0.078 0.494 - - 0.291 7.582 20.939 - - - - - - - - - - 0.007 322.295 32 Water Vapor Biodiesel Purification Water Vapor Condenser 0.002 - - - - 0.005 5.657 17.276 - - - - - - - - - - - 22.940 33 Biodiesel Biodiesel Purification Batch Test Tank 292.901 0.078 0.494 - - 0.286 1.925 3.663 - - - - - - - - - - 0.007 299.355 34 Glycerin Phase Process Biodiesel Processor MeOH Flash 3.733 0.006 0.400 - - 79.608 158.946 42.219 - - - 3.477 0.724 - - - 4.280 - 1.214 294.607

- - - 1.000 1.000 1.000 35 Methanol Vapor Biodiesel Processor MeOH Flash Methanol Condenser - - - - - 0.050 149.769 40.633 - - - - - - - - - - - 190.452 36 Glycerin Biodiesel Processor MeOH Flash Glycerin Tank 3.733 0.006 0.400 - - 79.559 9.177 1.586 - - - 3.477 0.724 - - - 4.280 - 1.214 104.156

Recovered Methanol Composition 0.009 (0.000) - - - 0.363 289.243 49.407 - - - - - - - - - - - 339.022


ATTACHMENT 7.05

2B Green Energy70 Million Liter Per Year Capacity

Biodiesel Process FacilityMaster Equipment List

Rev. 0 Page 1 of 16/28/2011 4:18 PM

Filename: 023-10-001-204 Master Equipment List.xlsx

Amount Unit HP RPM

E3 FullSpectrum Biodiesel Processor 100,000 LPD 2 Units

Raw Oil Filters 2 Semi-Continuous Units

Raw Oil Storage Tank No. 1 2,000,000 Liters 13.6 m Ø X 13.7 m H Flat Bottom, Dish or Flat Top

Raw Oil Storage Tank No. 2 2,000,000 Liters 13.6 m Ø X 13.7 m H Flat Bottom, Dish or Flat Top

Biodiesel Decanter 70,000 Liters 5.5 m Ø X 11 m H ASME Pressure Vessel

Sedimentation Tank 80,000 Liters 6.1 m Ø X 12 m H Flat Bottom, Dish or Flat Top

Biodiesel Storage Tank No. 1 2,000,000 Liters 13.6 m Ø X 13.7 m H Flat Bottom, Dish or Flat Top

Biodiesel Storage Tank No. 2 2,000,000 Liters 13.6 m Ø X 13.7 m H Flat Bottom, Dish or Flat Top

Glycerin Storage Tank 750,000 Liters 10.2 m Ø X 9.1 m H Flat Bottom, Dish or Flat Top

Methanol Storage Tank 1,000,000 Liters 10.9 m Ø X 10.7 m H Flat Bottom, Dish or Flat Top

Catalyst Storage Tank 300,000 Liters 7.55 m Ø X 6.7 m H Flat Bottom, Dish or Flat Top

Batch Test Tank No. 1 100,000 Liters 4.8 m Ø X 13.7 m H Flat Bottom, Dish or Flat Top

Batch Test Tank No. 2 100,000 Liters 4.8 m Ø X 13.7 m H Flat Bottom, Dish or Flat Top

Sweet Methanol Surge Tank 38,000 Liters 2.5 m Ø X 5 m H Flat Bottom, Dish or Flat Top

Reclaimed Methanol Storage Tank 100,000 Liters 5.3 m Ø X 4.6 m H Future Tank

Pre Treatment Tank No. 1 500,000 Liters 9.14 m Ø X 7.6 m H Future Tank

Pre Treatment Tank No. 2 500,000 Liters 9.14 m Ø X 7.6 m H Future Tank

Raw Oil Transfer Pump 250 LPM Centrifugal 15 1800

Raw Oil Charge Pump 157 LPM Centrifugal 10 1800

Methanol Charge Pump 27 LPM Gear 2 1800

Catalyst Charge Pump 1 LPM Gear 1 1800

Biodiesel Transfer Pump 11 LPM Centrifugal 2 1800

Biodiesel Load-Out Pump 1 LPM Centrifugal 1 1800

Glycerin Load-Out Pump 250 LPM Centrifugal 15 1800

Boiler Fuel Feed Pump 7 LPM Centrifugal 2 Pumps, 1 Backup 10 1800

Methanol Distillation System

Nitrogen Tank

Chiller System 150 HP 2 Chillers

Boiler System 200 HP 2 Boilers

Compressor System 2 Compressors

Cooling Tower System 2 Towers

Boiler Fuel Storage Tank 150,000 Liters 5.00 m Ø X 8.0 m H Flat Bottom, Dish or Flat Top

Equipment Number CommentsTypeSize Design

PressureDesign

TemperatureMaterial P&ID #Equipment NameSpecifications

Supplied By Cost ($)Motor Size Complexity

Factor Unit Cost ($/lb)


ATTACHMENT 7.06

ID Task Name Duration Start Finish

1 Engineering 86 days? Thu 9/1/11 Thu 12/29/112 Project General 36 days? Thu 9/1/11 Thu 10/20/113 Utilities 36 days? Thu 9/1/11 Thu 10/20/114 Electric 14 days? Thu 9/1/11 Tue 9/20/115 Water 22 days? Thu 9/1/11 Fri 9/30/116 Sewer 36 days? Thu 9/1/11 Thu 10/20/117 Fire Water 24 days? Thu 9/1/11 Tue 10/4/118 Process 18 days? Thu 9/1/11 Mon 9/26/119 Mass/Energy Balance 3.5 days? Thu 9/1/11 Tue 9/6/11

10 Process Flow Diagram 5 days? Tue 9/6/11 Tue 9/13/1111 Design Criteria 6 days? Tue 9/6/11 Wed 9/14/1112 P&ID's 18 days? Thu 9/1/11 Mon 9/26/1113 Civil/Structural 51 days? Thu 9/1/11 Thu 11/10/1114 Geotech Report 8 days? Thu 9/1/11 Mon 9/12/1115 Site Topographic Survey 7 days? Thu 9/1/11 Fri 9/9/1116 Site Civil/Grading Plan 12 days? Mon 9/12/11 Tue 9/27/1117 Underground Utilities 8 days? Wed 9/28/11 Fri 10/7/1118 Building Specification 3 days? Thu 9/1/11 Mon 9/5/1119 Building Information to Port Authority 0 days Mon 9/5/11 Mon 9/5/1120 Tank Farm Foundation & Containment 24 days? Wed 9/28/11 Mon 10/31/1121 Housekeeping Pads 8 days? Tue 11/1/11 Thu 11/10/1122 Processor Mounting Design 1.5 days? Tue 11/1/11 Wed 11/2/1123 Mechanical 44 days? Tue 9/27/11 Fri 11/25/1124 Site Layout 5 days? Tue 9/27/11 Mon 10/3/1125 Equipment List 6 days? Tue 9/27/11 Tue 10/4/1126 Specifications 40 days? Mon 10/3/11 Fri 11/25/1127 Tanks 2 days? Mon 10/3/11 Tue 10/4/1128 Boiler 2 days? Mon 10/3/11 Tue 10/4/1129 Pumps 3 days? Thu 10/13/11 Mon 10/17/1130 Tote Stations 1.5 days? Mon 10/3/11 Tue 10/4/1131 Compressed Air System 4 days? Mon 10/3/11 Thu 10/6/1132 Nitrogen System 4 days? Mon 10/3/11 Thu 10/6/1133 Chiller System 3 days? Mon 10/3/11 Wed 10/5/1134 Pressure and Vacuum Reliefs/N2 Padding V 5 days? Wed 10/5/11 Tue 10/11/1135 Flame Arresters 1 day? Wed 10/12/11 Wed 10/12/1136 Filters 5 days? Mon 10/3/11 Fri 10/7/1137 Tank Heaters 3 days? Wed 10/5/11 Fri 10/7/1138 Truck Loadout System 8 days? Tue 11/1/11 Thu 11/10/1139 Rail Loadout System 9 days? Tue 11/1/11 Fri 11/11/1140 Specs to Bid 8 wks? Mon 10/3/11 Fri 11/25/1141 General Arrangements 16 days? Tue 10/4/11 Tue 10/25/1142 Piping Plans 32 days? Fri 10/7/11 Mon 11/21/1143 Piping Specifications 4 days? Mon 10/3/11 Thu 10/6/1144 Pump Calculations 12 days? Tue 9/27/11 Wed 10/12/1145 Pipe Line List 5 days? Tue 9/27/11 Mon 10/3/1146 Pipe Support Racks 6 days? Wed 11/16/11 Wed 11/23/1147 Fire Protection Specification 4 days? Tue 9/27/11 Fri 9/30/1148 Fire Protection to Contractor 14 days? Mon 10/3/11 Thu 10/20/1149 Electrical 27 days? Wed 10/26/11 Thu 12/1/1150 Classified Area Plan 5 days? Wed 10/26/11 Tue 11/1/1151 One-Line Diagram 8 days? Wed 10/26/11 Fri 11/4/1152 MCC Layout 16 days? Mon 11/7/11 Mon 11/28/1153 Grounding/Lightnining Protection Plan 6 days? Wed 10/26/11 Wed 11/2/1154 Power/Instrumentation Plan 12 days? Mon 11/7/11 Tue 11/22/1155 Cable Schedule 7 days? Wed 11/23/11 Thu 12/1/1156 Instrumentation/Controls 28 days? Tue 11/22/11 Thu 12/29/1157 Instrument List 12 days Tue 11/22/11 Wed 12/7/1158 Bid Instrument List 10.5 days? Thu 12/8/11 Thu 12/22/1159 Bid Controls Configuration 16 days? Thu 12/8/11 Thu 12/29/1160 Permitting 72 days? Thu 9/1/11 Fri 12/9/1161 Air Quality Permit 11 wks? Thu 9/1/11 Wed 11/16/1162 Environmental Impact Assessment Registration 12.8 wks? Thu 9/1/11 Tue 11/29/1163 Watercourse & Wetland Alteration Permit 13 wks? Thu 9/1/11 Wed 11/30/1164 Boiler Permit 7.6 wks? Wed 10/5/11 Fri 11/25/1165 Electrical Wiring Permit 3 days? Tue 12/6/11 Thu 12/8/1166 Building Permit 17 days? Fri 11/11/11 Mon 12/5/1167 Misc. Permits 10 days? Mon 11/28/11 Fri 12/9/1168 Procurement 180 days? Thu 9/1/11 Wed 5/9/1269 Biodiesel Processor 180 days? Thu 9/1/11 Wed 5/9/1270 Processor 1 6 mons? Thu 9/1/11 Wed 2/15/1271 Processor 2 9 mons? Thu 9/1/11 Wed 5/9/1272 Building 4 mons? Tue 9/6/11 Mon 12/26/1173 Tanks 15.2 wks? Tue 10/25/11 Tue 2/7/1274 Boiler 12 wks? Tue 10/25/11 Mon 1/16/1275 Pumps 6 wks? Mon 11/7/11 Fri 12/16/11

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2B Green BioEnergyMoncton, New Brunswick

70 MILLION LITRE PER YEAR BIODIESEL PLANTPort of Dalhousie

Page 1

Project: Project Schedule.mppDate: Tue 6/28/11

ID Task Name Duration Start Finish

76 Tote Stations 2 wks? Mon 10/24/11 Mon 11/7/1177 Compressed Air System 8 wks? Thu 10/27/11 Wed 12/21/1178 Nitrogen System 12 wks? Thu 10/27/11 Wed 1/18/1279 Chiller System 14 wks? Wed 10/26/11 Tue 1/31/1280 Pressure and Vacuum Reliefs/N2 Padding Valves 9 wks? Tue 11/1/11 Mon 1/2/1281 Flame Arresters 8 wks? Wed 11/2/11 Tue 12/27/1182 Filters 16 wks? Fri 10/28/11 Thu 2/16/1283 Tank Heaters 12 wks? Fri 10/28/11 Thu 1/19/1284 Truck Loadout System 18 wks? Thu 12/1/11 Wed 4/4/1285 Rail Loadout System 18 wks? Fri 12/2/11 Thu 4/5/1286 Construction 90 days? Tue 12/6/11 Mon 4/9/1287 Mobilization 5 days? Tue 12/6/11 Mon 12/12/1188 Site Work 45 days? Tue 12/13/11 Mon 2/13/1289 Cut & Fill 11 days? Tue 12/13/11 Tue 12/27/1190 Underground Utilities 14 days? Wed 12/28/11 Mon 1/16/1291 Grading 24 days? Wed 12/28/11 Mon 1/30/1292 Piling 16 days? Wed 12/28/11 Wed 1/18/1293 Pile Caps 18 days? Thu 1/19/12 Mon 2/13/1294 Concrete 35 days? Tue 1/31/12 Mon 3/19/1295 Foundations 22 days? Tue 1/31/12 Wed 2/29/1296 Maintenance Pads 19 days? Wed 2/22/12 Mon 3/19/1297 Steel 63 days? Tue 12/13/11 Thu 3/8/1298 Fabrication 19 days? Tue 12/13/11 Fri 1/6/1299 Site Delivery 13 days Wed 12/28/11 Fri 1/13/12

100 Erection 39 days? Mon 1/16/12 Thu 3/8/12101 Equipment Installation 82 days? Tue 12/6/11 Wed 3/28/12102 Piping 61 days? Mon 1/16/12 Mon 4/9/12103 Instrumentation 61 days? Mon 1/16/12 Mon 4/9/12104 In-Line Devices 56 days? Mon 1/23/12 Mon 4/9/12105 Field Devices 37 days? Mon 1/16/12 Tue 3/6/12106 DCS 45 days? Mon 1/16/12 Fri 3/16/12107 Electrical 49 days? Fri 12/9/11 Wed 2/15/12108 Main Substation 14 days Fri 12/9/11 Wed 12/28/11109 Electrical Room 34 days Fri 12/9/11 Wed 1/25/12110 Tray & Conduit 28 days? Thu 12/29/11 Mon 2/6/12111 Wire & Cable 35 days? Thu 12/29/11 Wed 2/15/12112 Plant Phase 1 Mechanical Completion 0 days Fri 2/17/12 Fri 2/17/12113 Environment, Health, Safety & Security Final Audit 3 days Mon 2/20/12 Wed 2/22/12114 Handover to C&SU/Operations 3 days Thu 2/23/12 Mon 2/27/12115116 Commissioning & Start-Up (C&SU) 109 days? Tue 2/28/12 Fri 7/27/12117 Utility Systems Commissioning 17 days Tue 2/28/12 Wed 3/21/12118 Operations & Maintenance Training 9 days Tue 2/28/12 Fri 3/9/12119 Processor 1 - Commissioning/Start-up 2 wks? Tue 2/28/12 Mon 3/12/12120 Processor 2 - Commissioning/Start-up 2 wks? Thu 5/10/12 Wed 5/23/12121 Final Acceptance 7 days? Thu 7/19/12 Fri 7/27/12122 Approval of Operations 0 days Fri 7/27/12 Fri 7/27/12123 Close-Out 104 days Tue 3/13/12 Fri 8/3/12124 Evaluate the Business 5 days Mon 7/30/12 Fri 8/3/12125 Evaluate Performance 77 days Tue 3/13/12 Wed 6/27/12126 Operations 15 days? Mon 8/6/12 Fri 8/24/12127 Operating Trials 3 wks? Mon 8/6/12 Fri 8/24/12128 Approval of Operating Warranties 0 days Fri 8/24/12 Fri 8/24/12

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Page 2


ID Task Name

1 Engineering2 Project General3 Utilities4 Electric5 Water6 Sewer7 Fire Water8 Process9 Mass/Energy Balance10 Process Flow Diagram11 Design Criteria12 P&ID's13 Civil/Structural14 Geotech Report15 Site Topographic Survey16 Site Civil/Grading Plan17 Underground Utilities18 Building Specification19 Building Information to Port Authority20 Tank Farm Foundation & Containment21 Housekeeping Pads22 Processor Mounting Design23 Mechanical24 Site Layout25 Equipment List26 Specifications27 Tanks28 Boiler29 Pumps30 Tote Stations31 Compressed Air System32 Nitrogen System33 Chiller System34 Pressure and Vacuum Reliefs/N2 Padding V35 Flame Arresters36 Filters37 Tank Heaters38 Truck Loadout System39 Rail Loadout System40 Specs to Bid41 General Arrangements42 Piping Plans43 Piping Specifications44 Pump Calculations45 Pipe Line List46 Pipe Support Racks47 Fire Protection Specification48 Fire Protection to Contractor49 Electrical50 Classified Area Plan51 One-Line Diagram52 MCC Layout53 Grounding/Lightnining Protection Plan54 Power/Instrumentation Plan55 Cable Schedule56 Instrumentation/Controls57 Instrument List58 Bid Instrument List59 Bid Controls Configuration60 Permitting61 Air Quality Permit62 Environmental Impact Assessment Registration63 Watercourse & Wetland Alteration Permit64 Boiler Permit65 Electrical Wiring Permit66 Building Permit67 Misc. Permits68 Procurement69 Biodiesel Processor70 Processor 171 Processor 272 Building73 Tanks74 Boiler75 Pumps

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Page 3


ID Task Name

76 Tote Stations77 Compressed Air System78 Nitrogen System79 Chiller System80 Pressure and Vacuum Reliefs/N2 Padding Valves81 Flame Arresters82 Filters83 Tank Heaters84 Truck Loadout System85 Rail Loadout System86 Construction87 Mobilization88 Site Work89 Cut & Fill90 Underground Utilities91 Grading92 Piling93 Pile Caps94 Concrete95 Foundations96 Maintenance Pads97 Steel98 Fabrication99 Site Delivery

100 Erection101 Equipment Installation102 Piping103 Instrumentation104 In-Line Devices105 Field Devices106 DCS107 Electrical108 Main Substation109 Electrical Room110 Tray & Conduit111 Wire & Cable112 Plant Phase 1 Mechanical Completion113 Environment, Health, Safety & Security Final Audit114 Handover to C&SU/Operations115116 Commissioning & Start-Up (C&SU)117 Utility Systems Commissioning118 Operations & Maintenance Training119 Processor 1 - Commissioning/Start-up120 Processor 2 - Commissioning/Start-up121 Final Acceptance122 Approval of Operations123 Close-Out124 Evaluate the Business125 Evaluate Performance126 Operations127 Operating Trials128 Approval of Operating Warranties

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Page 4



ATTACHMENT 7.07

Summary2B Green Capital Estimate - 70mmlpy R1.xlsx Page 1 of 1

7/9/201111:14 AM

27-Jun-11Client: 2B Green BioEnergy

Location: Port of Dalhousie Project No.: 023-10-001-02CONSTRUCTION COST ESTIMATE

70 MMLPY Biodiesel Plant

Summary% of Const. SUB- BUDGET

DESCRIPTION Cost OWNER CONTR MAN TOTAL CONTRACT TOTALFURNISH FURNISH HOURS LABOR TOTAL

Site Work 7.8% $0 $1,537,810 11,686 $730,375 $125,000 $2,393,185Civil/Structural 0.0% $0 $0 - $0 $0 $0Process 49.5% $13,659,737 $502,941 14,230 $960,241 $0 $15,122,918Mechanical 0.7% $0 $69,050 2,200 $148,500 $0 $217,550Piping 8.3% $0 $1,244,700 17,934 $1,291,212 $0 $2,535,912Electrical 6.1% $0 $1,060,670 11,820 $809,684 $0 $1,870,354Instrumentation 3.4% $501,286 $140,796 5,009 $393,061 $0 $1,035,143Leasehold Improvement Costs 20.0% $193,925 $4,124,905 25,569 $1,785,702 $0 $6,104,532

Total Direct Cost $14,354,948 $8,680,871 88,447 $6,118,774 $125,000 $29,279,593Contractor's Indirects 2.4% $739,982Contractor's Fees 1.8% $556,419

Total Construction Cost $30,575,995

Engineering 6.7% $2,049,572Environmental Assessment 0.7% $220,000Site Geotechnical Investigation & Surveys 0.2% $75,000Environmental or Legislative Costs 0.4% $120,000Capitalized Spares 0.6% $173,617Taxes 0.0% $0Construction Insurance 1.4% $439,194Freight 1.1% $345,537

Total Indirects $3,422,920

Sub-Total Direct and Indirects $33,998,915Contingency 9.6% $2,927,959

Total PP&E $36,926,874Escalation <Not Included>Capitalized Interest <Not Included>Deferred Start-Up Costs <Not Included>Working Capital <Not Included>Operator Training & Start-Up <Not Included>

Grand Total $36,926,874

Site Work2B Green Capital Estimate - 70mmlpy R1.xlsx Page 1 of 1




Site Work Detail MATERIAL CONTRACTOR LABOR SUB- BUDGET

EQUIPMENT DESCRIPTION QTY. UNIT UNIT OWNER CONTR MH MAN RATE TOTAL CONTRACT TOTALNUMBER PRICE FURNISH FURNISH UNIT HOURS TOTAL

Excavation & BackfillU/G Utilities 500 m³ 33 16,350 0.5 250.0 62.50 15,625 31,975 Excavation (Cut & Fill) 10,000 m³ 16 157,000 0.5 5,000.0 62.50 312,500 469,500 Fill (Engineered) 10,000 m³ 20 196,200 0.5 5,000.0 62.50 312,500 508,700

Environmental - - - Landscaping - - 50,000 50,000 Site Beautification - - -

- - - Utilities:

Electrical 1 lot 75,000 75,000 0.0 - 75,000 Water & Fire protection 1 lot 285,000 285,000 0.0 - 285,000 Sanitary Sewer 1 lot 18,500 18,500 0.0 - 18,500 Storm Sewer 1 lot 135,000 135,000 0.0 - 135,000

Paving - Roads and parking areas 2,600 m² 115 299,000 0.1 156.0 62.50 9,750 308,750

Truck & Rail Load/Unload PadsContainment Slab, w/curb 80 m³ 327 26,160 6.0 480.0 62.50 30,000 56,160 Sump 2 ea 4,500 9,000 60.0 120.0 62.50 7,500 16,500 Oil Separator 2 ea 9,000 18,000 60.0 120.0 62.50 7,500 25,500 Vault 2 ea 26,000 52,000 280.0 560.0 62.50 35,000 87,000

PlantSecurity 1 lot 150,000 150,000 - 150,000 Access Control 1 lot 75,000 75,000 - 75,000 Fire Alarm 1 lot 25,600 25,600 - 25,600 Fencing 1 lot - 75,000 75,000

Site Work Total $0 $1,537,810 11,686 $730,375 $125,000 $2,393,185

Structural2B Green Capital Estimate - 70mmlpy R1.xlsx Page 1 of 1




Structural Work Detail MATERIAL CONTRACTOR LABOR SUB- BUDGET


Structural Work Total $0 $0 0 $0 $0 $0

Process2B Green Capital Estimate - 70mmlpy R1.xlsx Page 1 of 2




Process Work Detail MATERIAL CONTRACTOR LABOR SUB- BUDGET


Field-Erected Tanks - West Tank FarmFeedstock, 2,000,000 L, 13.6 dia x 13.7, CS, API 650 2 ea 315,000 $630,000 120.0 240.0 67.50 16,200 646,200 Biodiesel, 2,000,000 L, 13.6 dia x 13.7, CS, API 650 2 ea 315,000 $630,000 120.0 240.0 67.50 16,200 646,200 Glycerin, 750,000 L, 10.2 dia x 9.1, CS, API 650 1 ea 178,000 $178,000 90.0 90.0 67.50 6,075 184,075

Field-Erected Tanks - North Tank FarmMethanol, 1,000,000 L, 10.9 dia x 10.7, CS, API 650 1 ea 235,000 $235,000 100.0 100.0 67.50 6,750 241,750 Catalyst Storage Tank, 300,000 L, 7.5 dia x 6.7, SS, API 650 1 ea 98,000 $98,000 75.0 75.0 67.50 5,063 103,063 Batch Test, 100,000 L, 4.8 dia x 13.7, CS, API 650 1 ea 48,000 $48,000 90.0 90.0 67.50 6,075 54,075 Decanter, 70,000 L, 5.5 dia x 11, CS, ASME VIII 1 ea 78,000 $78,000 110.0 110.0 67.50 7,425 85,425 Sedimentation, 80,000 L, 6.1 dia x 12, CS, API 650 1 ea 39,000 $39,000 90.0 90.0 67.50 6,075 45,075 Boiler Fuel Tank 1 ea 35,000 $35,000 75.0 75.0 67.50 5,063 40,063

Shop-Fabricated Tanks & Vessels

Tank HeatersFin-tube coil, 75' dia., CS 9 ea 12,650 $113,850 32.0 288.0 67.50 19,440 133,290

Insulation - Tanks Feedstock Tanks (2 @ 13.6 dia. x 13.7) 4,329 m² 45 194,803 0.8 3,463.2 67.50 233,764 428,567 Biodiesel Tanks (2 @ 13.6 dia. x 13.7) 4,329 m² 45 194,803 0.8 3,463.2 67.50 233,764 428,567 Glycerin Tanks (1 @ 10.2 dia. x 9.1) 842 m² 45 37,874 0.8 673.3 67.50 45,449 83,323 Biodiesel Holding Tanks (1 @ 9.1 dia. x 7.6) 572 m² 45 25,755 0.8 457.9 67.50 30,906 56,662 Feedstock Holding Tanks (1 @ 9.1 dia. x 7.6) 572 m² 45 25,755 0.8 457.9 67.50 30,906 56,662 Miscellaneous equipment (assume 5% of preceding) 532 m² 45 23,950 1.2 638.7 67.50 43,109 67,059

Tank Vent & Blanketing SystemN2 Blanket valves, 50 mm 4 ea 2,960 $11,840 8.0 32.0 67.50 2,160 14,000 Vac/Pressure Relief valves 11 ea 3,600 $39,600 8.0 88.0 67.50 5,940 45,540 Emergency Vents/Gauge Hatch 11 ea 7,800 $85,800 12.0 132.0 67.50 8,910 94,710 Flame arresters 5 ea 879 $4,395 6.0 30.0 67.50 2,025 6,420 Desiccant Breathers 11 ea 659 $7,249 4.0 44.0 67.50 2,970 10,219

Biodiesel ProcessorE3 FullSpectrum 2 ea 4,412,000 $8,824,000 120.0 240.0 67.50 16,200 8,840,200

Methanol Distillation SystemDistillation Column w/Condensers, reboiler & Controls 1 lot 1,320,000 $1,320,000 240.0 240.0 67.50 16,200 1,336,200

Feedstock FiltersFeedstock Final Filter Skid 1 ea 85,253 $85,253 220.0 220.0 67.50 14,850 100,103 Feedstock roughing, duplex 1 ea 3,500 $3,500 16.0 16.0 58.50 936 4,436 Product, final filter, duplex 1 ea 8,500 $8,500 16.0 16.0 58.50 936 9,436 Misc. Strainers & Filters 1 lot 25,000 $25,000 80.0 80.0 67.50 5,400 30,400

Process2B Green Capital Estimate - 70mmlpy R1.xlsx Page 2 of 2




Process Work Detail MATERIAL CONTRACTOR LABOR SUB- BUDGET


Truck Loading SystemCustody Transfer System 1 lot 65,000 $65,000 80.0 80.0 67.50 5,400 70,400 Loading System 1 lot 89,350 $89,350 240.0 240.0 67.50 16,200 105,550 Vapor Control 1 lot 35,000 $35,000 120.0 120.0 67.50 8,100 43,100

Rail Loading SystemCustody Transfer System 1 lot 65,000 $65,000 80.0 80.0 67.50 5,400 70,400 Loading System 1 lot 165,000 $165,000 360.0 360.0 67.50 24,300 189,300 Vapor Control 1 lot 35,000 $35,000 120.0 120.0 67.50 8,100 43,100

Ship/Barge Loading SystemCustody Transfer System 1 lot 65,000 $65,000 80.0 80.0 67.50 5,400 70,400 Loading Arm 1 lot 186,000 $186,000 480.0 480.0 67.50 32,400 218,400

UtilitiesAir Compressor 1 ea 69,900 $69,900 120.0 120.0 67.50 8,100 78,000 Nitrogen Generator 1 ea 85,000 $85,000 380.0 380.0 67.50 25,650 110,650 Chillers 1 ea 89,500 $89,500 120.0 120.0 67.50 8,100 97,600 Boilers 1 ea 135,000 $135,000 360.0 360.0 67.50 24,300 159,300

LaboratoryEquipment Allowance 1 lot 75,000 $75,000 - 75,000

Process Work Total $13,659,737 $502,941 14,230 $960,241 $0 $15,122,918

Mechanical2B Green Capital Estimate - 70mmlpy R1.xlsx Page 1 of 1




Mechanical Work Detail MATERIAL CONTRACTOR LABOR SUB- BUDGET


UtilitiesComponent Assembly & Installation 1 lot 3,500 3,500 500.0 500.0 67.50 33,750 37,250 Building Ventilation 1 lot 25,000 25,000 380.0 380.0 67.50 25,650 50,650 Ventilation Ductwork 1 lot 18,600 18,600 460.0 460.0 67.50 31,050 49,650 Misc. Mechanical Asssemblies 1 lot 8,000 8,000 220.0 220.0 67.50 14,850 22,850

LaboratoryVent Hood Ducting 1 lot 1,850 1,850 180.0 180.0 67.50 12,150 14,000 HVAC 1 lot 5,600 5,600 100.0 100.0 67.50 6,750 12,350

Control RoomHVAC 1 lot 6,500 6,500 360.0 360.0 67.50 24,300 30,800

Mechanical Work Total $0 $69,050 2,200 $148,500 $0 $217,550

Piping2B Green Capital Estimate - 70mmlpy R1.xlsx Page 1 of 1




Piping Work Detail MATERIAL CONTRACTOR LABOR SUB- BUDGET


Piping 3/4" sch 40 CS 8 cft 437 3,496 12.6 100.8 72.00 7,258 10,754 1" sch 40 CS 12 cft 565 6,780 12.6 151.2 72.00 10,886 17,666 1 1/2" sch 40 CS 5 cft 598 2,990 14.8 74.0 72.00 5,328 8,318 2" sch 40 CS 60 cft 1,197 71,820 16.6 996.0 72.00 71,712 143,532 4" sch 40 CS 75 cft 3,497 262,275 25.0 1,875.0 72.00 135,000 397,275 6" sch 40 CS 10 cft 6,137 61,370 35.0 350.0 72.00 25,200 86,570

Hangers & supports Assume 20' average distance, 4" avg. size, guided slides 850 ea 165 140,250 3.6 3,060.0 72.00 220,320 360,570

Fittings & valvesElls 1,360 lt 15 20,264 0.6 816.0 72.00 58,752 79,016 Tees 340 lt 37 12,427 1.2 408.0 72.00 29,376 41,803 Reducers 510 lt 24 11,985 0.7 357.0 72.00 25,704 37,689 Flanges 850 lt 19 16,023 1.3 1,105.0 72.00 79,560 95,583 Gate valves 221 lt 395 87,295 2.0 442.0 72.00 31,824 119,119 Check valves 136 lt 405 55,080 2.0 272.0 72.00 19,584 74,664

Gaskets & Bolt kits (assume .75 per flange) 425 ea 30 12,750 1.0 425.0 72.00 30,600 43,350

Piping insulation Assume 70% of pipe is insulated. Use 4" pipe as avearage for lot. 2" dense fiberglass W/ .016 Aluminum 11,900 ft 2.85 33,915 0.2 2,618.0 72.00 188,496 222,411

MiscellaneousPressure Indicators, w/ isolation valve 9 ea 150 1,350 0.5 4.5 72.00 324 1,674 Temperature Indicators 8 ea 150 1,200 0.5 4.0 72.00 288 1,488

Ship/Barge LoadPipe, 6" 65 cft 6,137 398,905 35.0 2,275.0 72.00 163,800 562,705 Insulation 65 cft 550 35,750 25.0 1,625.0 72.00 117,000 152,750 Heat Trace 65 cft 135 8,775 15.0 975.0 72.00 70,200 78,975

Piping Work Total $0 $1,244,700 17,934 $1,291,212 $0 $2,535,912

Electrical2B Green Capital Estimate - 70mmlpy R1.xlsx Page 1 of 1




Electrical Work Detail MATERIAL CONTRACTOR LABOR SUB- BUDGET


- - - Site Electrical - - -

SWGR 1 EA 100,000 100,000 160.0 160.0 68.50 10,960 110,960 MCCs 1 EA 60,000 60,000 160.0 160.0 68.50 10,960 70,960 Pwr Pnl 600A 1 EA 6,000 6,000 40.0 40.0 68.50 2,740 8,740 Panel Board 3 EA 4,200 12,600 24.0 72.0 68.50 4,932 17,532 UPS 1 EA 35,000 35,000 80.0 80.0 68.50 5,480 40,480 Power Cable (est) 8,800 LF 2.950 25,960 0.084 739.2 68.50 50,635 76,595 Control Cable (est) 6,500 LF 1.450 9,425 0.065 422.5 68.50 28,941 38,366 Cable Tray 20,000 SF 8.45 169,000 0.082 1,640.0 68.50 112,340 281,340 Ltg 335 EA 695 232,825 3.5 1,172.5 68.50 80,316 313,141 Poles 20 EA 1,500 30,000 32.0 640.0 68.50 43,840 73,840 Disc Outlet 4 EA 850 3,400 8.0 32.0 68.50 2,192 5,592 Gnd Equip ( Grid) 40,000 SF 1.24 49,600 0.024 960.0 68.50 65,760 115,360 Misc Elect Equip 16 EA 1,000 16,000 24.0 384.0 68.50 26,304 42,304 Elect Heat Trace 6,800 LF 8.95 60,860 0.4 2,448.0 68.50 167,688 228,548

Truck Loading System - - - Cable to Loading System 1 lot 26,000 26,000 300.0 300.0 68.50 20,550 46,550 Wire & Conduit 1 lot 35,200 35,200 360.0 360.0 68.50 24,660 59,860

- - - Rail Loading System - - -

Cable to Loading System 1 lot 26,000 26,000 300.0 300.0 68.50 20,550 46,550 Wire & Conduit 1 lot 35,200 35,200 360.0 360.0 68.50 24,660 59,860

- - - Ship Loading System - - -

Cable to Loading System 1 lot 54,000 54,000 560.0 560.0 68.50 38,360 92,360 Wire & Conduit 1 lot 45,000 45,000 620.0 620.0 68.50 42,470 87,470

- - - Utilities - - -

Air Compressor Power 1 lot 7,600 7,600 130.0 130.0 68.50 8,905 16,505 Nitrogen System Power 1 lot 7,000 7,000 80.0 80.0 68.50 5,480 12,480 Chiller System Power 1 lot 7,000 7,000 80.0 80.0 68.50 5,480 12,480 Boiler System Power 1 lot 7,000 7,000 80.0 80.0 68.50 5,480 12,480

- - -

Electrical Work Total $0 $1,060,670 11,820 $809,684 $0 $1,870,354

Instrumentation2B Green Capital Estimate - 70mmlpy R1.xlsx Page 1 of 3




Instrumentation Work Detail MATERIAL CONTRACTOR LABOR SUB- BUDGET


Tank FarmFeedstock Tank

Level Transmitter 2 ea 2,096 $4,192 8.0 16.0 76.20 1,219 5,411 Temperature Transmitter 2 ea 1,172 $2,344 8.0 16.0 76.20 1,219 3,563 Pressure Transmitter 2 ea 1,684 $3,368 8.0 16.0 76.20 1,219 4,587 Level Switch 2 ea 1,672 $3,344 8.0 16.0 76.20 1,219 4,563 Misc. Gauges 2 lots 645 $1,290 4.0 8.0 76.20 610 1,900 Tubing & Fittings 2 lots 1,350 2,700 16.0 32.0 76.20 2,438 5,138

Biodiesel TankLevel Transmitter 2 ea 2,096 $4,192 8.0 16.0 76.20 1,219 5,411 Temperature Transmitter 2 ea 1,172 $2,344 8.0 16.0 76.20 1,219 3,563 Flow Transmitter 1 ea 6,550 $6,550 12.0 12.0 76.20 914 7,464 Flow Control Valve 1 ea 4,334 $4,334 12.0 12.0 76.20 914 5,248 Level Switch 2 ea 1,672 $3,344 8.0 16.0 76.20 1,219 4,563 Misc. Gauges 2 lots 645 $1,290 4.0 8.0 76.20 610 1,900 Tubing & Fittings 2 lots 1,350 2,700 16.0 32.0 76.20 2,438 5,138

Glycerin TankLevel Transmitter 1 ea 2,096 $2,096 8.0 8.0 76.20 610 2,706 Level Switch 1 ea 1,672 $1,672 8.0 8.0 76.20 610 2,282 Temperature Transmitter 1 ea 1,172 $1,172 8.0 8.0 76.20 610 1,782 Flow Transmitter 1 ea 6,550 $6,550 12.0 12.0 76.20 914 7,464 Flow Control Valve 1 ea 4,334 $4,334 12.0 12.0 76.20 914 5,248 Misc. Gauges 1 lots 645 $645 4.0 4.0 76.20 305 950 Tubing & Fittings 1 lots 1,350 1,350 16.0 16.0 76.20 1,219 2,569

Methanol TankLevel Transmitter 1 ea 2,096 $2,096 8.0 8.0 76.20 610 2,706 Temperature Transmitter 1 ea 1,172 $1,172 8.0 8.0 76.20 610 1,782 Flow Transmitter 1 ea 6,550 $6,550 12.0 12.0 76.20 914 7,464 Flow Control Valve 1 ea 4,334 $4,334 12.0 12.0 76.20 914 5,248 Tank Relief/Pressure Regulator 1 ea 3,500 $3,500 6.0 6.0 76.20 457 3,957 Level Switch 1 ea 1,672 $1,672 8.0 8.0 76.20 610 2,282 Misc. Gauges 1 lots 645 $645 4.0 4.0 76.20 305 950 Tubing & Fittings 1 lots 1,350 1,350 16.0 16.0 76.20 1,219 2,569

Boiler Fuel TankLevel Transmitter 1 ea 2,096 $2,096 8.0 8.0 76.20 610 2,706 Level Switch 1 ea 1,672 $1,672 8.0 8.0 76.20 610 2,282 Misc. Gauges 1 lots 645 $645 4.0 4.0 76.20 305 950

Catalyst TankLevel Transmitter 1 ea 2,096 $2,096 8.0 8.0 76.20 610 2,706 Temperature Transmitter 1 ea 1,172 $1,172 8.0 8.0 76.20 610 1,782 Flow Transmitter 1 ea 6,550 $6,550 12.0 12.0 76.20 914 7,464 Flow Control Valve 1 ea 4,334 $4,334 12.0 12.0 76.20 914 5,248 Tank Relief/Pressure Regulator 1 ea 3,500 $3,500 6.0 6.0 76.20 457 3,957 Level Switch 1 ea 1,672 $1,672 8.0 8.0 76.20 610 2,282 Misc. Gauges 1 lots 645 $645 4.0 4.0 76.20 305 950







Tubing & Fittings 1 lots 1,350 1,350 16.0 16.0 76.20 1,219 2,569 Decanter

Level Transmitter 1 ea 2,096 $2,096 8.0 8.0 76.20 610 2,706 Temperature Transmitter 1 ea 1,172 $1,172 8.0 8.0 76.20 610 1,782 Level Switch 1 ea 1,672 $1,672 8.0 8.0 76.20 610 2,282 Misc. Gauges 1 lots 645 $645 4.0 4.0 76.20 305 950 Tubing & Fittings 1 lots 1,350 1,350 16.0 16.0 76.20 1,219 2,569

SedimentationLevel Transmitter 1 ea 2,096 $2,096 8.0 8.0 76.20 610 2,706 Level Switch 1 ea 1,672 $1,672 8.0 8.0 76.20 610 2,282 Misc. Gauges 1 lots 645 $645 4.0 4.0 76.20 305 950 Tubing & Fittings 1 lots 1,350 1,350 16.0 16.0 76.20 1,219 2,569

Oil FilterDifferential Pressure Switch 2 ea 950 $1,900 4.0 8.0 76.20 610 2,510

Biodiesel FilterDifferential Pressure Switch 1 ea 950 $950 4.0 4.0 76.20 305 1,255

Block Valve, 6" 18 ea 5,800 $104,400 6.0 108.0 76.20 8,230 112,630 Field Termination Panel 3 ea 13,500 40,500 46.0 138.0 76.20 10,516 51,016 Control Wiring 9,000 ft 1.35 12,150 0.120 1,080.0 76.20 82,296 94,446 Reclaimed Methanol Storage Tank

Process AreaAdditive Tote & Metering PumpControl Wiring 280 ft 2.70 756 0.120 33.6 76.20 2,560 3,316

Truck Loading SystemGround/Overfill Protection System 1 lot 35,000 $35,000 80.0 80.0 76.20 6,096 41,096 Block Valve, 6" 6 ea 6,850 $41,100 12.0 72.0 76.20 5,486 46,586 Field Termination Panel 1 ea 15,000 15,000 38.0 38.0 76.20 2,896 17,896 Control Wiring 3,800 ft 1.35 5,130 0.120 456.0 76.20 34,747 39,877

Rail Loading SystemGround/Overfill Protection System 1 lot 35,000 $35,000 80.0 80.0 76.20 6,096 41,096 Block Valve, 6" 6 ea 6,850 $41,100 12.0 72.0 76.20 5,486 46,586 Field Termination Panel 1 ea 15,000 15,000 38.0 38.0 76.20 2,896 17,896 Control Wiring 3,800 ft 1.35 5,130 0.120 456.0 76.20 34,747 39,877

Ship/Barge Loading SystemGround/Overfill Protection System 1 lot 35,000 $35,000 80.0 80.0 76.20 6,096 41,096 Block Valve, 6" 8 ea 6,850 $54,800 12.0 96.0 76.20 7,315 62,115 Field Termination Panel 1 ea 15,000 15,000 38.0 38.0 76.20 2,896 17,896 Control Wiring 8,800 ft 1.35 11,880 0.120 1,056.0 76.20 80,467 92,347

UtilitiesAir Compressor

Pressure Transmitter 1 ea 1,684 $1,684 8.0 8.0 76.20 610 2,294







Misc. Gauges 1 lots 645 $645 4.0 4.0 76.20 305 950 Tubing & Fittings 1 lots 1,350 1,350 16.0 16.0 76.20 1,219 2,569 Control Wiring 400 ft 1.35 540 0.120 48.0 76.20 3,658 4,198

Nitrogen SystemPressure Transmitter 1 ea 1,684 $1,684 8.0 8.0 76.20 610 2,294 Misc. Gauges 1 lots 645 $645 4.0 4.0 76.20 305 950 Tubing & Fittings 1 lots 1,350 1,350 16.0 6.0 76.20 457 1,807 Control Wiring 400 ft 1.35 540 0.120 48.0 76.20 3,658 4,198

Chiller SystemTemperature Transmitter 1 ea 1,172 $1,172 8.0 8.0 76.20 610 1,782 Misc. Gauges 1 lots 645 $645 4.0 4.0 76.20 305 950 Tubing & Fittings 1 lots 1,350 1,350 16.0 6.0 76.20 457 1,807 Control Wiring 800 ft 1.35 1,080 0.120 96.0 76.20 7,315 8,395

Boiler SystemTemperature Transmitter 1 ea 1,172 $1,172 8.0 8.0 76.20 610 1,782 Pressure Transmitter 1 ea 1,684 $1,684 8.0 8.0 76.20 610 2,294 Misc. Gauges 1 lots 645 $645 4.0 4.0 76.20 305 950 Tubing & Fittings 1 lots 1,350 1,350 16.0 6.0 76.20 457 1,807 Control Wiring 400 ft 1.35 540 0.120 48.0 76.20 3,658 4,198

Process Control SystemComputers 2 ea 2,500 $5,000 0.5 1.0 76.20 76 5,076 Process Control Network 1 lot 8,650.00 $8,650 32.0 32.0 130.00 4,160 12,810 PLC Hardware 1 lot 15,000.00 $15,000 180.0 180.0 130.00 23,400 38,400 Control Software 1 lot 6,000.00 $6,000 0.0 130.00 - 6,000

Instrumentation Work Total $501,286 $140,796 5,009 $393,061 $0 $1,035,143

Leasehold2B Green Capital Estimate - 70mmlpy R1.xlsx Page 1 of 2




Leasehold Improvement Costs MATERIAL CONTRACTOR LABOR SUB- BUDGET


Foundations Tank & Equipment Foundations 780 m³ 327 255,060 6.0 4,680.0 69.85 326,898 581,958 Tanks & Equipment Pilings 140 ea 1,600 224,000 - 224,000 Pipe Bridge Foundations 120 m³ 327 39,240 6.0 720.0 69.85 50,292 89,532 Pipe Bridge Piling 64 ea 1,600 102,400 0.0 - 102,400 West Containment Slab, w/ walls & curb 1,250 m³ 327 408,750 6.0 7,500.0 69.85 523,875 932,625 North Containment Slab, w/ walls & curb 880 m³ 327 287,760 6.0 5,280.0 69.85 368,808 656,568 Housekeeping Pads 180 m³ 285 51,300 5.0 900.0 69.85 62,865 114,165

Structural SteelPipe racks 108 tons 4,400 475,200 25.0 2,700.0 69.85 188,595 663,795 Miscellaneous supports 65 tons 4,400 286,000 25.0 1,625.0 69.85 113,506 399,506 Catwalks & Access Platforms 48 tons 5,800 278,400 36.0 1,728.0 69.85 120,701 399,101

Buildingby Port of Dalhousie 9,200 m²

Office, Control Room & Lab Space 680 m² 1,080 734,400 0.0 69.85 - 734,400 Hazardous Chemical Room 389 m² 1,450 564,050 0.0 69.85 - 564,050

Untiltled Items 20% 1 lot 416,365 416,365 0.0 - 416,365 Pipe supports - 0.0 - - Other - 0.0 - -

Pumps Feedstock, Truck Receiving, 1,300 lpm, 15 hp 1 ea 11,500 $11,500 18.0 18.0 67.50 1,215 12,715 Methanol/Methylate, Truck Receiving, 570 lpm, 10 hp 1 ea 9,400 $9,400 18.0 18.0 67.50 1,215 10,615 Biodiesel Loadout, 1,800 lpm, 20 hp 1 ea 13,280 $13,280 18.0 18.0 67.50 1,215 14,495 Glycerin Loadout, 1,250 lpm, 15 hp 1 ea 11,500 $11,500 18.0 18.0 67.50 1,215 12,715 Feedstock Supply Pump, 300 lpm, 5 hp 2 ea 8,100 $16,200 18.0 36.0 67.50 2,430 18,630 Methanol Supply Pump, 100 lpm, 1.5 hp 2 ea 4,100 $8,200 18.0 36.0 67.50 2,430 10,630 Sodium Methylate Supply Pump, 20 lpm 1 ea 4,500 $4,500 18.0 18.0 67.50 1,215 5,715 Biodiesel to Storage Pump, 1,500 lpm, 15 hp 1 ea 11,500 $11,500 18.0 18.0 67.50 1,215 12,715 Sump Pump, verical shaft, 150 lpm 5 hp 2 ea 8,100 $16,200 18.0 36.0 67.50 2,430 18,630

Feedstock Charge, 175 gpm @ 150' TDH, 7.5 hp 1 ea 12,450 12,450 18.0 18.0 76.88 1,384 13,834 Feedstock Heat Recovery 150 gpm @ 150' TDH, 7.5 hp 1 ea 12,450 12,450 18.0 18.0 76.88 1,384 13,834 Decanted Biodiesel Transfer, 170 gpm @ 74 TDH, 7.5 hp 1 ea 11,500 11,500 12.0 12.0 76.88 923 12,423 Decanted Glycerin Transfer, 9 gpm @ 54 TDH, 1 hp 1 ea 4,800 4,800 12.0 12.0 76.88 923 5,723 Raw Biodiesel Return, 9 gpm @ 64 TDH, 1.5 hp 1 ea 6,000 6,000 12.0 12.0 76.88 923 6,923 Methylate Transfer, 5 gpm @ 10 psi, air driven 1 ea 1,300 1,300 2.0 2.0 76.88 154 1,454 Methanol Solvent, 5 gpm @ 10 psi, air driven 1 ea 1,300 1,300 2.0 2.0 76.88 154 1,454 Deactivation Agent, 3 gpm @ 10 psi, air driven 1 ea 695 695 2.0 2.0 76.88 154 849

Blowers

Tank Vent Recovery 1 ea 2,650 $2,650 24.0 24.0 67.50 1,620 4,270

Leasehold2B Green Capital Estimate - 70mmlpy R1.xlsx Page 2 of 2




Leasehold Improvement Costs MATERIAL CONTRACTOR LABOR SUB- BUDGET


MiscellaneousInstrument Air Drier System 1 ea 38,500 $38,500 38.0 38.0 67.50 2,565 41,065

Hazardous Storage RoomVentilation 1 lot 1,980 1,980 80.0 80.0 67.50 5,400 7,380

Leasehold Costs Total $193,925 $4,124,905 25,569 $1,785,702 $0 $6,104,532


ATTACHMENT 7.08

S:\Marketing\E3 Process Documents\Biodiesel - Batch\E3 FullSpectrum Process.docx

1008 Western Avenue, Suite 307 Seattle, WA 98104 Phone: (206) 462-3600 e-Mail: [email protected] Fax: (206) 462-3599 Website: www.e3energypartners.com

E3 FullSpectrum™ Biodiesel Process

The E3 FullSpectrum™ biodiesel process is a batch process designed for maximum flexibility in processing a wide variety of oils and fats into biodiesel. The process is developed around modular units of 100,000 liters per day that can be paralleled to provide a variety of plant sizes and configurations. The process can be customized with a variety of pre-treatment and purification options that allow acceptance of low quality oils with the capability to process them into high quality biodiesel with relatively high yields. The key advantages to the process are:

Ability to blend and process a wide variety of oils and fats. Batch processing for maximum flexibility Modular design for managed growth Water-free purification High level of energy integration & methanol recovery Post-treatment to fine tune properties and provide better cold-flow properties. Highly automated with low consumable and operating costs per unit produced

Options:

Degumming, drying & filtering feedstock oils & fats Feedstock pretreatment from 0 to12% and / or 12% to 100% FFA Integrated FOG rendering (trap to brown grease) Advanced purification via distillation

Process Item Description Basic Plant

Basic Plant Components Tank Farm, Rail Load/Unload, Truck Load/Unload, Pre-Treatment, Transesterification, Methanol Recovery, Purification, Vent Recovery, Thermal Driver, and Utilities.

Plant Turndown 5:1 Plant Single Line Size (Module) 100,000 liters per day; 26,420 gallons / day

16,000 MT / yr.; 9.2 MMGY Number of Lines One to Six Yield 96% Minimum

Basic Plant Process Details: Oil Pre-Treatment Oil is treated to reduce free fatty acids, dried to remove water, and filtered to

remove solids. Acid esterification is used for FFA below 12%, and glycerol esterification is used for FFA levels from 12 to 100%.

Transesterification The pre-treated oil is processed in a single stage batch reactor, using high-shear mixing. The use of high shear mixers allows for a faster initial reaction rate, and quicker separation of glycerol. The process also allows for re-treatment of off-spec product, and recycling of glycerol for catalyst use reduction.

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Process Item Description

Catalyst A sodium methylate solution in methanol is used as the transesterification reaction catalyst. Acid esterification uses a sulfuric acid catalyst, and glycerol esterification uses a metal oxide catalyst.

Methanol Recovery Methanol is recovered through flash evaporation. Methanol is recovered separately from the acid esterification, transesterification and glycerin recovery stages..

Methanol Rectification Recovered methanol vapor is rectified in a packed column to separate water, and provide purified methanol back to the process.

Purification Purification options include processing of the biodiesel through an ion-exchange column to remove impurities, and distillation for biodiesel from low quality feedstocks that might have difficulty meeting ASTM specifications..

Post-Treatment A cold-filtering system provides a biodiesel that will meet ASTM cold-soak specifications.

Thermal Driver The high temperatures required for the glycerol esterification pre-treatment process, and the distillation purification make hot oil the most cost effective thermal source for the plant. Steam is an option for the portions of the process that do not require higher temperatures.

Energy Integration The energy from the plant hot streams have been closely matched to cold streams for pre-heating. The plant heat is tightly integrated to provide maximum efficiency.

Vent Gas Collection All tank and process vents are collected and combusted in the hot oil burner. Safety Plant process areas are identified by hazard classification, and all energy

sources within that area are either explosion-proof, or intrinsically safe. Feedstock:

Oil Type Any filtered, degummed oil or fat, either recycled or virgin. Free Fatty Acid (FFA), Max. % No limit on FFA content (depending on pre-treatment option selected) Water Content, Max. % 5% Unsaponifiables, Max. % No limit, but will reduce yield. Phosphorus, Max. 50 PPM Sulfur, Max. 25 PPM (Optional sulfur treatments are available for higher levels)

Yield (1 MT pure oil): (Glycerol esterification pre-treatment with ion-exchange purification) Biodiesel, kg 980 Crude Glycerol, kg 136

Utilities (per 1 MT Product): Electrical Power, kWh 26 Natural Gas, GJ 0.85 Plant Water, litre 0 Compressed Air, Nm³ 6.2 Nitrogen, Nm³ 2.2

Consumables (per 1 MT Product): Methanol. kg 107 Sodium Methylate, kg 4.6 Ion Exchange Resin, kg 1

Emissions (per 1 MT Product): Methanol Vapor, kg 0.00894 Water Vapor, kg 21.44 Solids, kg 5.30

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Example Plant Layout

Typical Process General Arrangement

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Rendering of Example Plant Layout – Aerial View

Rendering of Example Plant Layout – Street View