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AIN08-W-06, METHANE RECOVERY IN WASTEWATER TREATMENT

SUMATERA UTARA, INDONESIA

UNFCCC Clean Development Mechanism Simplified Project Design Document

for Small Scale Projects

DOCUMENT ID: AIN08-W-06 VER 1, 21 APR 2008

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CLEAN DEVELOPMENT MECHANISM PROJECT DESIGN DOCUMENT FORM (CDM-SSC-PDD)

Version 03 - in effect as of: 22 December 2006

CONTENTS A. General description of the small scale project activity B. Application of a baseline and monitoring methodology C. Duration of the project activity / crediting period D. Environmental impacts E. Stakeholders’ comments

Annexes Annex 1: Contact information on participants in the proposed small scale project activity Annex 2: Information regarding public funding Annex 3: Baseline information

Annex 4: Monitoring Information

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Revision history of this document Version Number

Date Description and reason of revision

01 21 January 2003

Initial adoption

02 8 July 2005 • The Board agreed to revise the CDM SSC PDD to reflect guidance and clarifications provided by the Board since version 01 of this document.

• As a consequence, the guidelines for completing CDM SSC PDD have been revised accordingly to version 2. The latest version can be found at <http://cdm.unfccc.int/Reference/Documents>.

03 22 December 2006

• The Board agreed to revise the CDM project design document for small-scale activities (CDM-SSC-PDD), taking into account CDM-PDD and CDM-NM.

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SECTION A. General description of small-scale project activity A.1 Title of the small-scale project activity: AIN08-W-06, Methane Recovery in Wastewater Treatment, Sumatera Utara, Indonesia, Version 1, 21/04/2008 A.2. Description of the small-scale project activity: Purpose: This project will recover methane caused by the decay of biogenic matter in the effluent stream of an existing palm oil processing mill by introducing methane recovery and combustion to the existing anaerobic effluent treatment system (lagoons). Explanation of GHG emission reductions: The proposed project activities will reduce GHG emissions in an economically sustainable manner, and will result in other environmental benefits, such as improved water quality and reduced odour. In simple terms, the project proposes to move from a high-GHG-emitting open air lagoon, to a lower-GHG-emitting anaerobic digester with capture and combustion of the resulting biogas. Contribution to sustainable development: Worldwide, agricultural operations are becoming progressively more intensive to realize the economies of production and scale. The pressure to become more efficient drives significant operational similarities between facilities of a “type,” as inputs, outputs, practices, and technology have become similar around the world. This is especially true in palm oil operations. Untreated, or raw, palm oil mill effluent (POME) is 100 times more polluting than domestic sewage. The Biological Oxygen Demand (BOD) of raw POME averages approximately 25,000 mg/liter.1 In a single year, the entire Indonesian palm oil industry produced POME equivalent to the domestic sewage of 20 million people, or one-tenth of the country’s total population in 1999.2 Because POME is quite concentrated, its handling and disposal can create profound environmental consequences, such as greenhouse gas emissions, odour, and water/land contamination (including seepage, runoff, and over application). The project will have positive effects on the local environment by improving air quality through the reduction of odor and cleaner emissions. The project will be installed with an extensive monitoring system, and is designed to comply with all the local environmental regulations.

1 Maheswaran and Singam (1977) as cited in African Journal of Agricultural Research Vol. 2 (12), p.657, http://www.academicjournals.org/AJAR/PDF/Pdf2007/Dec/Ojonoma%20and%20Nnennaya.pdf 2 http://www.cspinet.org/palmoilreport/PalmOilReport.pdf

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A.3. Project participants:

Name of Party involved (*) (host) indicates a host

Party

Private and/or public entity(ies) project participants

(*) (as applicable)

Kindly indicate if the party involved wishes to be considered as project

participant (Yes/No)

Indonesia (host) PT AES AgriVerde Indonesia No

Switzerland AES AgriVerde Ltd. No

A.4. Technical description of the small-scale project activity: A.4.1. Location of the small-scale project activity: A.4.1.1. Host Party(ies): The Host Party for this project is Indonesia. A.4.1.2. Region/State/Province etc.: The project is located within the Sumatera Utara, Indonesia. A.4.1.3. City/Town/Community etc: The project site is shown in Figures 1 and 2 with specifics detailed in Table 1. A.4.1.4. Details of physical location, including information allowing the unique identification of this small-scale project activity : The project location is shown in Figures 1 and 2 and details are provided in Table 1. Short descriptions of sites are provided below:

PKS PT Sago Nauli has the following site in Sumatera Utara, Indonesia:

• PKS PT Sago Nauli (76-76) is a palm oil mill with a processing capacity of 30 tonnes per hour. This facility processes approximately 105,063 tonnes of Fresh Fruit Bunches (FFBs) per year, but expects to increase its output due to mill expansion. Additionally, the mill is currently conducting some composting that removes a small amount of POME from a lagoon that is not included in this or any other CDM project. The mill, which is in regulatory compliance, operates approximately 14 hours per day, 6 days per week, 25 days per month, and 300 days per year. A system of open lagoons is used to process POME effluent: one cooling, two anaerobic lagoons, one facultative lagoon, and one polishing lagoon. The anaerobic lagoons measures approximately 80m x 35m x 5m and 109m x 108m x 5m, respectively. The facultative lagoon measures approximately 190m x 70m x 4m. Lagoon depth in some locations may occasionally vary due to sludge build-up. As a result, these lagoons are subject to sludge removal as needed.

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Figure 1. Project Activity Site in Sumatera Utara, Indonesia

PROJECT DESIGN DOCUMENT FORM (CDM-SSC-PDD) - Version 03 CDM – Executive Board

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Table 1 – Detailed physical location / identification of project site(s)

Site Name (Site ID) Address Town/State Contact Phone GPS

PKS PT Sago Nauli (76-76)

Desa Sinunukan, Kecamatan Batahan

Sumatera Utara, Indonesia Yohannes Ivan +62-61-4150935 N0 28.202

E99.13471


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A.4.2. Type and category(ies) and technology/measure of the small-scale project activity: The project activity described in this document is classified as a Type III, Other Project Activities, Category III.H., Ver. 9, option iv, Methane recovery in wastewater treatment.3 This project activity will capture and combust methane gas produced from the anaerobic portion of an existing wastewater treatment system.

The project activity utilizes a simple, effective and reliable technology to capture lagoon-produced biogas: installing sealed covers over existing anaerobic POME lagoons to create an anaerobic digester system. Each cover will consist of a synthetic high-density polyethylene (HDPE) geo-membrane which is sealed by means of strip-to-strip welding and a peripheral anchor trench dug around the perimeter of the existing lagoon. The welded seams will be tested to ensure air-tight coupling between all HDPE pieces. In addition, lagoon berms will be upgraded, if necessary, to ensure secure anchoring. HDPE is an excellent product for large applications requiring UV, ozone, and chemical resistance and because of these attributes is one of the most commonly used geo-membranes worldwide. This covering approach effectively enables capture/combustion of 100% of the biogas produced in these lagoons. The digesters incorporate other features to enhance long-term reliability and efficiency including a sludge handling system that enables sludge removal without breaking the digester’s air-tight seal. Other features that will be installed depending on site specific conditions is an effluent recirculation and/or multiple agitators to gently turn over the POME, simulating the natural atmospheric and solar turbulence which will be blocked by the HDPE covers. Since the project developer considers digester design elements as proprietary information, specific design information will be made available to the validating and verifying DOEs. POME will continue to flow from the anaerobic treatment section to facultative and algae treatment lagoons so that the effluents discharge requirements can be met. The captured biogas will be routed to one or more high temperature, enclosed flares to destroy methane gas as it is produced. Biogas will be accurately metered using a thermal mass flow meter that has two sensing elements: a velocity sensor and a temperature sensor that automatically corrects for changes in gas temperature. The transducer electronics heats the velocity sensor to a constant temperature differential above the gas temperature and measures the cooling effect of the gas flow. The meter runs on DC power and includes a UPS back-up system to provide for the possibility of power outages. This meter type offers distinct advantages over standard flow meters including direct mass flow sensing for temperature and pressure compensation, high accuracy and repeatability for low-pressure gas flow measurement applications, outstanding rangeability, lower flow blockage and pressure drop than conventional meters, and no moving parts. The meter measures the mass flow and automatically converts to normalized volumetric output (NCMA). The biogas flow meter is normalized to 0 degrees Celsius at 1 ATM and calibrated in NCMH units by the manufacturer. Standard density conversion factors are established by the manufacturer. The flaring combustion system is automated to ensure that all biogas that exits the digester and passes through a meter and flare is combusted. A continuous flare ignition system with redundant electrodes ensures methane is combusted whenever biogas is present at the flare. This continuous ignition system is powered by a solar module (solar-charged battery system) that does not require external power. With a fully charged battery, the module will provide power to the igniter for up to two weeks without sunlight. The flare includes thermocouples to monitor flare temperature, which is measured and recorded more often than hourly. The component parts are verified functional on a periodic basis in accordance with manufacturer and other technical specifications.

3 http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7


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Maintenance procedures have been developed to ensure proper handling and disposition of the digester sludge. The disposal of digester sludge will not vary from the baseline scenario. Technology and know-how transfer: The materials and labour used in this project are sourced from the host country whenever possible. When unavailable in the host country, resources may be acquired from other countries. A multi-faceted approach will be implemented to ensure that technology transfer proceeds smoothly, including a methodical process for identifying and qualifying appropriate technology/services providers, transferring the manufacture and maintenance of certain subassemblies to local manufacturers, supervision of the complete installation, staff training, ongoing monitoring (by both site and project developer personnel) and development/implementation of a Monitoring Plan (by the project developer). By working closely with the project on a day-to-day basis, the project developer will ensure that all installed equipment is properly operated and maintained, and will carefully monitor the data collection and recording process. Moreover, by working with the mill site’s staff over many years, the project developer will ensure that site personnel acquire appropriate expertise and resources to operate the system on an ongoing/continuous basis.

A.4.3 Estimated amount of emission reductions over the chosen crediting period:

Estimated Emission Reduction over the chosen crediting period

Years Annual estimation of emission reductions in tonnes of CO2e

Year1: 2008 - 2009 6,583 Year2: 2009 - 2010 9,924 Year3: 2010 - 2011 14,962 Year4: 2011 - 2012 22,890 Year5: 2012 - 2013 22,890 Year6: 2013 - 2014 22,890 Year7: 2014 - 2015 22,890 Total estimated reductions (tonnes CO2e)

123,028

Total number of crediting years 7

Annual average of estimated reductions over the crediting period (tonnes CO2e)

17,575

A.4.4. Public funding of the small-scale project activity: No public funding is being provided for this project.


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A.4.5. Confirmation that the small-scale project activity is not a debundled component of a large scale project activity: Based on the Compendium of guidance on the debundling for SSC project activities(EB36, Annex 27)4 this project is not debundled according to the following definition: “A proposed small-scale project activity shall be deemed to be a debundled component of a large project activity if there is a registered small-scale CDM project activity or an application to register another small-scale CDM project activity:

(a) With the same project participants; (b) In the same project category and technology/measure; and (c) Registered within the previous 2 years; and (d) Whose project boundary is within 1 km of the project boundary of the proposed small-scale activity

at the closest point.” SECTION B. Application of a baseline and monitoring methodology B.1. Title and reference of the approved baseline and monitoring methodology applied to the small-scale project activity: The project activity applies the UNFCCC-approved small scale methodology AMS III.H., Ver. 9, Methane recovery in wastewater treatment.5 The project is a small scale project because it comprises methane recovery from agro-industries and aggregate emission reductions will not exceed 60 kt CO2eq from all type III components of the project activity annually. B.2 Justification of the choice of the project category: The simplified methodologies are appropriate because the project activity site is considered an agro-industry and GHG emissions calculations can be estimated using internationally accepted IPCC guidance.

The proposed project activity will recover methane from biogenic organic matter in wastewaters according to option (iv) of the methodology:

Introduction of methane recovery and combustion to an existing anaerobic wastewater treatment system such as anaerobic reactor, lagoon, septic tank or an on site industrial plant 6.

This project introduces methane recovery and combustion to an existing wastewater treatment system (a system of anaerobic and facultative lagoon(s)). This simplified baseline methodology is applicable to this project activity because without the proposed project activity, methane from the existing anaerobic treatment system would continue to be emitted into the atmosphere. Based on historical FFB processing rates and baseline estimates, the estimated emission reductions of the project activity will not exceed 60 kt CO2e in any year of the crediting period as shown in Section A.4.3. 4http://cdm.unfccc.int/Reference/Guidclarif/ssc/methSSC_guid17_v01.pdf 5 http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7 6 http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7


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B.3. Description of the project boundary:

As stated in the AMS III-H methodology, the project boundary “is the physical, geographical site where the wastewater and sludge treatment takes place”.

Sources influenced by the project are included in the project boundary while sources not influenced by the project are excluded. For this project, the boundary is the physical, geographical site of the PKS PT Sago Nauli facility that includes the two anaerobic lagoons (both of which are covered using HDPE to enable the (project’s) capture and combustion of lagoon generated methane)). Sludge treatment is not affected by the implementation of the project activity, and will be disposed of in the same manner as it was prior to the project activity.

Palm Oil production

Final discharge to land or waterway

Other lagoon(s) not part of treatment system (i.e. facultative, aerobic, etc.)

Waste treatment system Flare

POME

Treated POME

Treated POME

Biogas

Figure 2 – Project Boundary

B.4. Description of baseline and its development: The amount of methane that would be emitted to the atmosphere in the absence of the project activity can be estimated by referring to UNFCCC-approved methodology AMS III.H, version 9, Methane recovery in wastewater treatment. The baseline scenario applicable to this project is in accordance with paragraph 23, option iv of the methodology:

iv. The existing anaerobic wastewater treatment system without methane recovery and combustion;


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As assessment of the palm oil facility determined that a system of open lagoons are used to treat POME. This is the most common practice in Indonesian palm oil mills7. Subsequent to treatment in the system of lagoons, the treated POME is normally either:8:

• Applied to land or • Directed to waterways

At this site, treated POME is applied to waterway. The facility was also found to comply with current effluent discharge standards. B.5. Description of how the anthropogenic emissions of GHG by sources are reduced below those that would have occurred in the absence of the registered small-scale CDM project activity: Anthropogenic GHGs, including methane, are released into the atmosphere via decomposition of POME. Currently, this biogas is not collected or destroyed. The proposed project activity intends to improve current wastewater management practices. These changes will result in the mitigation of anthropogenic GHG emissions, specifically the recovery of methane, by controlling the lagoon’s decomposition processes and collecting and combusting the biogas.

There are no existing, pending, or planned national regulatory requirements that govern GHG emissions from agro-industry operations (specifically, palm oil mill processing activities) as outlined in this PDD. The project participants have solicited information regarding this issue during numerous conversations with local and state government officials and through legal representation and have determined there is no regulatory impetus for producers to upgrade current wastewater treatment systems beyond the recommended open air anaerobic lagoon(s).

According to the Non-binding best practice examples to demonstrate addtionality for SSC project activities (EB35, Annex 34),9 “project participants shall provide an explanation to show that the project activity would not have occurred anyway due to at least one of the following barriers”:

• Investment barrier: a financially more viable alternative to the project activity would have led to higher emissions;

• Access-to-finance barrier: the project activity could not access appropriate capital without consideration of the CDM revenues;

• Technological barrier: a less technologically advanced alternative to the project activity involves lower risks due to the performance uncertainty or low market share of the new technology adopted for the project activity and so would have led to higher emissions;

• Barrier due to prevailing practice: prevailing practice or existing regulatory or policy requirements would have led to implementation of a technology with higher emissions;

• Other barriers such as institutional barriers or limited information, managerial resources, organizational capacity, or capacity to absorb new technologies.

The most relevant barrier(s) which have prevented this project activity from being implemented without the assistance of CDM are as follows:

• Investment barriers (most significant barrier): This wastewater treatment approach is considered one of the most advanced systems in the world. Producers in few countries have implemented this

7 http://cdm.unfccc.int/UserManagement/FileStorage/ECSPMWBQE5ZFYX9EJ1OWPAN41O579E 8 http://www.menlh.go.id/archive.php?action=cat&cat=7 9 http://cdm.unfccc.int/Reference/Guidclarif/methSSC_guid15_v01.pdf


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type of technology on a widespread basis because of the high costs of associated materials and ongoing maintenance. Though costs vary according to required lagoon size and other factors, initial costs to install an anaerobic digester system can run in the tens of thousands of US dollars10. The Indonesian palm oil industry views the installation of waste treatment systems as a means to satisfy statutory effluent discharge requirements, not a potential revenue source. Although “anaerobic digestion is a versatile biological treatment technology yielding methane as a useful bioenergy”, the majority of mills continue to use pond or lagoon systems. These existing waste treatment systems adhere to Indonesian government requirements and are significantly lower in capital and operating costs than anaerobic digestion technology.11 Implementing this project without the assistance of CDM does not provide the mill owner with the positive economic returns to justify or even partially offset the expenses.12

• Technological barriers: Anaerobic digester systems must be sized to handle projected effluent volumes with a Hydraulic Retention Time (HRT) consistent with extracting all methane from the POME. Moreover, operations and maintenance requirements involved with this technology, including the means to maintain pond circulation (once they are covered), maintaining biochemical equilibrium within the digester(s) and a detailed monitoring (including equipment and material maintenance) program to maintain system performance levels must also be considered13. There is a need for skilled and experienced operators and the availability of such personnel locally is limited as such biogas systems are still relatively rare.14

• Barriers due to prevailing practice: The current lagoon-based treatment system is considered the standard operating practice in palm oil mills in Indonesia15. Despite numerous changes to maximum discharge standards over the years, the combination of anaerobic lagoons and aerobic/facultative lagoons remains able to meet the current permitted discharge levels for land application or waterway discharge. The primary wastewater management priority for most palm oil mills is to simply maintain compliance with local effluent discharge regulations.

While past practices cannot predict future events, it is worth noting that the site included in this project activity has been in existence for a number of years, during which time the prevailing wastewater management practice has been a system of open lagoons. As a result, there is no regulatory requirement for facilities to alter their current practices.

10 http://www.mrec.org/pubs/25145.pdf 11 http://www.cogen3.net/doc/countryinfo/malaysia/TechnicalEconomicAnalysisCHPPalmEffluent_BG.pdf 12 http://www.jst.go.jp/asts/asts_j/files/ppt/12_ppt.pdf 13 http://www.mrec.org/biogas/adgpg.pdf p.39-42. 14 http://www.bothends.org/strategic/061211_Biomass%20case%20study%20Indonesia.pdf 15 http://cdm.unfccc.int/UserManagement/FileStorage/ECSPMWBQE5ZFYX9EJ1OWPAN41O579E


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B.6. Emission reductions:

B.6.1. Explanation of methodological choices: Baseline Emissions The amount of methane that would be emitted to the atmosphere in the absence of the project activity can be estimated by referring to UNFCCC-approved methodology AMS III.H, version 9, Methane recovery in wastewater treatment. The baseline scenario applicable to this project is in accordance with paragraph 23, option iv of the methodology:

iv) The existing anaerobic wastewater treatment system without methane recovery and combustion;

For option iv, the methodology requires baseline emissions be calculated as per the formulas below, with MCF lower values from Table III.H.1 to be used.

Equation 1: Total baseline emissions16

BEy = MEPy,ww,bl * GWP_CH4 + MEPy,s,treatment * GWP_CH4 Where:

BEy Baseline emissions in the year y, tonnes CO2e

MEPy,ww,bl Methane emission potential of the anaerobic wastewater treatment plant in the baseline situation in the year y, tonnes

MEPy,s,treatment Methane emission potential of the sludge treatment system in the year y, tonnes

GWP_CH4 Global warming potential of methane

The following equations (Equations 2 and 3) are used to determine the values applied in Equation 1: Equation 2: Baseline emission potential of the wastewater treatment plant17

MEPy,ww,bl = Qy,ww *∑(CODy,removed,i * Bo,ww * MCFww,treatment,i) Where:

MEPy,ww,bl Methane emission potential of the anaerobic wastewater treatment plant in the baseline situation in the year y, tonnes

Qy,ww Volume of wastewater treated in the year “y” (m3)

CODy,removed,i Chemical oxygen demand removed by the anaerobic wastewater treatment system “i” in the baseline situation in the year “y” (tonnes/ m3)

Bo,ww Methane producing capacity of the wastewater

16 Adapted from UNFCCC methodology AMS-III.H (Methane recovery in wastewater treatment), V.9, http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7 17 Adapted from UNFCCC methodology AMS-III.H (Methane recovery in wastewater treatment), V.9, http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7


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MCFww, treatment,i Methane correction factor for the existing anaerobic wastewater treatment system “i” (MCF lower value in Table III.H.1)

Equation 3: Baseline emission potential of the sludge treatment system18

MEPy,s,treatment = Sy, untreated * DOCy,s,untreated * DOCf * F * 16/12 * MCFs,treatment

Where:

MEPy,s,treatment Methane emission potential of the sludge treatment system in the year “y” (tonnes)

Sy,untreated Amount of untreated sludge generated in the year “y” (tones)

DOCy,s, untreated Degradable organic content of untreated sludge generated in the year y (fraction). It shall be measured by sampling and analysis of the sludge produced, and estimated ex-ante using the IPCC default values of 0.05 for domestic sludge (wet basis, considering a default dry matter content of 10 percent) or 0.09 for industrial sludge (wet basis, assuming dry matter content of 35 percent).

DOCf Fraction of DOC dissimilated to biogas

F Fraction of CH4 in landfill gas

MCFs,treatment Methane correction factor for the sludge treatment system that will be equipped with methane recovery and combustion/utilization/flare equipment (MCF lower value in Table III.H.1)

18 Adapted from UNFCCC methodology AMS-III.H (Methane recovery in wastewater treatment), V.9, http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7


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Project Activity Emissions

As defined by the methodology, project activity emissions consist of: (i) CO2 emissions on account of power used by the project activity facilities. Emission factors for grid

electricity or diesel fuel use as the case may be shall be calculated as described in category AMS I.D.;

(ii) Methane emissions on account of inefficiency of the wastewater treatment and presence of degradable organic carbon in treated wastewater;

(iii) Methane emissions from the decay of the final sludge generated by the treatment systems; (iv) Methane fugitive emissions on account of inefficiencies in capture and flare systems; (v) Methane emissions resulting from dissolved methane in the treated wastewater effluent. (vi) Where relevant, emissions due to the upgrading and compression of biogas (cases covered under

paragraph 2 (b) and 2 (c)). (vii) Where relevant, emissions due to physical leakage from the dedicated piped network for transport of

upgraded biogas to the end users (cases covered under paragraph 2 (c ii)). In this case, items (iii), (v), (vi), and (vii) are not applicable to the project activity emissions for the following reasons:

• Item (iii) may be neglected since the methodology states in paragraph 12 where PEy,s,final, “If the sludge is controlled combusted, disposed in a landfill with methane recovery, or used for soil application, this term can be neglected, and the final disposal of the sludge shall be monitored during the crediting period.” Therefore, PEy,s,final can be neglected since sludge disposition in this project is soil application.

• Item (v) is “only considered for project activities involving measures described in cases (i), (v), and (vi) of paragraph 1”. Since this project recovers methane by technology option (iv), PEy,dissolved does not need to be calculated.

• Item (vi) may be neglected since this only applies to “(cases covered under paragraph 2 (b) and 2 (c))”. Since those cases are not applicable to this project, PEy,upgrading can be neglected.

• Item (vii) may be neglected since this only applies to “(cases covered under paragraph 2 (c ii))”.

Since that case is not applicable to this project, PEy,leakage, pipeline can be neglected. For this project activity (an anaerobic digester), estimated project emissions are determined as follows: Equation 4: Total project activity emissions19

PEy =PEy,power + PEy,ww,treated + PEy,fugitive Where:

PEy Project activity emissions in the year “y” (tCO2e)

PEy,power Emissions from electricity or diesel consumption in the year “y”

PEy,ww,treated Emissions from degradable organic carbon in treated wastewater in the year “y”

PEy,fugitive Emissions from methane release in capture and utilization/combustion/flare systems in the year “y”



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The following equations (Equations 5 through 7) are used to determine the values applied in Equation 4.

Emissions from electricity consumption

According to the methodology, paragraph 13 states: “Project activity emissions from electricity consumption are determined as per the procedures described in AMS I.D. The energy consumption of all equipment/devices installed by the project activity, inter alia facilities for upgrade and compression, filling of bottles, distribution and the final end use of biogas shall be included. For project activity emissions from fossil fuel consumption the emission factor for the fossil fuel shall be used (tCO2/tonne). Local values are to be used, if local values are difficult to obtain, IPCC default values may be used. If recovered methane is used to power auxiliary equipment of the project it should be taken into account accordingly, using zero as its emission factor.” PEy, power details are provided in Annex 3.

Equation 5: Emissions from degradable organic carbon in treated wastewater20

PEy,ww,treated = Qy,ww * GWP_CH4 * Bo,ww * CODy,ww,treated * MCFww,final Where:

PEy,ww,treated Emissions from degradable organic carbon in treated wastewater in the year “y”




CODy, ww, treated Chemical oxygen demand of the final treated wastewater discharged into sea, river or lake in the year “y” (tonnes/m3)

MCFww, final Methane correction factor based on type of treatment and discharge pathway of the wastewater (fraction) (MCF higher value in Table III.H.1)

Emissions from methane release in capture and utilization/combustion/flare systems

In the project activity, fugitive emissions through capture and utilization/combustion/flare inefficiencies in the anaerobic sludge treatment (PEy,fugitive,s) are not calculated since sludge is not subject to any methane capture and flare system.

Therefore, total fugitive emissions (PEy,fugitive) consists solely of fugitive emissions through capture and utilization/combustion/flare inefficiencies in the anaerobic wastewater treatment (PEy,fugitive,ww).



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Equation 6: Fugitive emissions through capture and utilization/combustion/flare inefficiencies in the anaerobic wastewater treatment21

PEy,fugitive,ww = (1-CFEww) *MEPy,ww,treatment *GWP_CH4

Where:

PEy,fugitive,ww Fugitive emissions through capture and utilization/combustion/flare inefficiencies in the anaerobic wastewater treatment in the year “y” (tCO2e)

CFEww Capture and utilization/combustion/flare efficiency of the methane recovery and combustion/utilization equipment in the wastewater treatment

MEPy,ww,treatment Methane emission potential of the wastewater treatment plant in the year “y” (tonnes)


Equation 7: Methane emission potential of the wastewater treatment plant22

MEPy,ww,treatment = Qy,ww * Bo,ww * ∑j CODy,removed,j * MCFww,j Where:

MEPy,ww,treatment Methane emission potential of the wastewater treatment plant in the year y, tonnes


CODy,removed,j Chemical oxygen demand removed by the treatment system “j” of the project activity equipped with methane recovery in the year “y” (tonnes/ m3)


MCFww,j Methane correction factor for the wastewater treatment system “j” equipped with methane recovery and combustion/flare/utilization equipment (MCF higher value in Table III.H.1)

Leakage

In accordance with the methodology, leakage calculations are not required since the technology being employed in this project is not transferred from or to another activity.

21 Adapted from UNFCCC methodology AMS-III.H (Methane recovery in wastewater treatment), V.9, http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7 22 Adapted from UNFCCC methodology AMS-III.H (Methane recovery in wastewater treatment), V.9, http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7


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Equation 8: Estimated emission reductions23

For the purposes of estimation, emission reductions are calculated as the difference between the baseline emission and the sum of the project emission and leakage. In accordance with the methodology, actual calculation of emission reductions during the crediting period will be “based on the amount of methane recovered and fuelled or flared, that is monitored ex-post”.

ERy =BEy –(PEy + Leakagey) Where:

ERy Emission reductions (tCO2e/year)

BEy Baseline emissions (tCO2e/year)

PEy Project emissions (tCO2e/year)

Leakagey Leakage emissions (tCO2e/year)

B.6.2. Data and parameters that are available at validation: Accurate data collection is essential. The subject palm oil processing facility maintains extensive FFB production and processing records to manage operations and to maximize productivity and profitability. AES AgriVerde uses some data collected from this system. AES AgriVerde has a rigorous QA/QC system that ensures data security and data integrity. Spot audits of data collection activities will be conducted on a regular basis. Project activity data related uncertainties will be reduced by applying sound data collection quality assurance and quality control procedures. Data / Parameter: GWP_CH4 Data unit: Description: Global Warming Potential of Methane Source of data used: Refer to AMS III-H, V.9 methodology Value applied: 21 Justification of the choice of data or description of measurement methods and procedures actually applied:

Comments: Data / Parameter: Qy,ww

Data unit: m3

Description: Volume of wastewater treated in the year y Source of data used: Calculated based on facility records Value applied: See Annex 3 Justification of the choice of data or description of measurement methods and procedures actually applied:

Determined by multiplying the FFB production by the conversion factor for FFB to POME. The conversion factor is verified by a third party on an annual basis.

Comments: 23 Adapted from UNFCCC methodology AMS-III.H (Methane recovery in wastewater treatment), V.9, http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7


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Data / Parameter: Bo,ww Data unit: kg CH4 / kg COD Description: Methane producing capacity of the treated wastewater Source of data used: IPCC default value for domestic wastewater as cited in AMS III H, V.9

methodology Value applied: 0.21 Justification of the choice of data or description of measurement methods and procedures actually applied:

Comments: Data / Parameter: DOCf Data unit: Fraction Description: DOC dissimilated to biogas Source of data used: IPCC default value as cited in AMS III H, V.9 methodology Value applied: 0.5 Justification of the choice of data or description of measurement methods and procedures actually applied:

Comments: Data / Parameter: F Data unit: Fraction Description: Fraction of CH4 in landfill gas Source of data used: IPCC default value as cited in AMS III H, V.9 methodology Value applied: 0.5 Justification of the choice of data or description of measurement methods and procedures actually applied:

Comments: Data / Parameter: MCFww,treatment,i Data unit: Fraction Description: Methane correction factor for the existing anaerobic wastewater treatment

system “i” Source of data used: IPCC default (lower) value from Table III.H.1 in AMS III H, V.9


The current type of wastewater treatment and discharge pathway or system to which this project will be applied from Table III.H.1 is Anaerobic deep lagoon (depth more than 2 metres).

Comments:


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Data / Parameter: MCFww,j

Data unit: Fraction Description: Methane correction factor for the wastewater treatment system equipped

with methane recovery and combustion/flare/utilization equipment Source of data used: IPCC default (higher) value from Table III.H.1 in AMS III H, V.9


The current type of wastewater treatment and discharge pathway or system to which this project will be applied from Table III.H.1 is Anaerobic deep lagoon (depth more than 2 metres)

Comments: Data / Parameter: MCFww,final Data unit: Fraction Description: Methane correction factor based on type of treatment and discharge

pathway of the wastewater Source of data used: IPCC default (higher) value from Table III.H.1 in AMS III H, V.9


The type of treatment and discharge pathway of the treated wastewater from Table III.H.1 is Aerobic treatment, poorly managed or overloaded.

Comments: Data / Parameter: MCFs,treatment Data unit: Fraction Description: Methane correction factor for the sludge treatment system that will be

equipped with methane recovery and combustion/utilization/flare equipment

Source of data used: Refer to AMS III H, V.9 methodology Value applied: 1.0 Justification of the choice of data or description of measurement methods and procedures actually applied:

This value is applied to both baseline and project equations since the baseline practice of disposing of the sludge via land application will not change and will continue to be practiced during the project activity. Paragraph 41 of the methodology permits methane emissions from anaerobic decay of the final sludge to be neglected “because the sludge is controlled combusted, disposed in a landfill with methane recovery, or used for soil application, then the end-use of the final sludge will be monitored during the crediting period.”

Comments:


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Data / Parameter: CFEww Data unit: Fraction Description: Capture and utilization/combustion/flare efficiency of the methane

recovery and combustion/utilization equipment in the wastewater treatment

Source of data used: Default value specified in AMS III H., V.9 methodology Value applied: 0.9 Justification of the choice of data or description of measurement methods and procedures actually applied:

Comments: Data / Parameter: CODy,ww,treated

Data unit: Tonnes/m3

Description: Chemical oxygen demand of the final treated wastewater discharged into sea, river or lake in the year “y”

Source of data used: Site Data Value applied: See Annex 3 Justification of the choice of data or description of measurement methods and procedures actually applied:

Comments: Data / Parameter: CODy,removed,i


Description: Chemical oxygen demand removed by the anaerobic wastewater treatment system “i” in the baseline situation in the year “y”


Comments: Data / Parameter: CODy,removed,j


Description: Chemical oxygen demand removed by the treatment system “j” of the project activity equipped with methane recovery in the year “y”


Comments:


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Data / Parameter: PEy,power

Data unit: tCO2e

Description: Emissions from electricity or diesel consumption in the year y Source of data used: Site Data Value applied: See Annex 3 Justification of the choice of data or description of measurement methods and procedures actually applied:

Comments:

Data / Parameter: DCH4,y

Data unit: kg/m3

Description: Density factor of methane Source of data used: Manufacturer specified value for continuous flow meter Value applied: Justification of the choice of data or description of measurement methods and procedures actually applied:

The biogas flow meter is normalized to 0 degrees Celsius at 1 ATM and calibrated in NCMH units by the manufacturer. Standard density conversion factors are established by the manufacturer

Comments: B.6.3 Ex-ante calculation of emission reductions:

Baseline emissions are calculated using Equations 1 through 3 in Section B.6.1. Table 8. Baseline Emissions

2008-2009 2009-2010 2010-2011 2011-2015365 550 829 1,250

0 0 0 021 21 21 21

7,662 11,551 17,414 26,254

Year 1 2 3 4 5 6 7Expected Growth%

0% 51% 51% 51% 0% 0% 0%

Baseline Emissions, (Waste Water) (tCO2e/year)

7,662 11,551 17,414 26,254 26,254 26,254 26,254 141,643

Total Baseline Emissions,

(tCO2e/year)7,662 11,551 17,414 26,254 26,254 26,254 26,254 141,643

YearSago Nauli (76-76)

Total

Sago Nauli (76-76)

Methane emission potential of untreated wastewater in tonnes CH4/yr (MEPy,ww,bl)Methane emission potential of untreated sludge in tonnes CH4/yr (MEPy,s,treatment)Global warming potential of methane (GWP_CH4)

Total annual baseline emissions in tonnes of CO2e (BEy)

Project emissions are calculated using Equations 4 through 7 in Section B.6.1.


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Table 9. Project Activity Emissions

2008-2009 2009-2010 2010-2011 2011-20150 0 0 0

48 72 109 820 0 0 0

1,031 1,555 2,344 3,2821,079 1,627 2,453 3,364

Year 1 2 3 4 5 6 7Expected Growth %

0% 51% 51% 37% 0% 0% 0%

Project Emissions (tCO2e/year)

1,079 1,627 2,453 3,364 3,364 3,364 3,364 18,615

Total

Emissions through methane release in capture and flare systems (PEy,fugitive)Total annual project emissions (PEy)

Sago Nauli (76-76)

Sago Nauli (76-76)

Emissions through electricity or diesel consumption (PEy,power)Emissions through degradable organic carbon in treated wastewater (PEy,ww,treated)Emissions through anaerobic decay of the final sludge produced (PEy,s,final)

Year

Since the technology used does not consist of equipment from another activity nor is the existing equipment transferred to another activity, leakage does not need to be considered as per the methodology.

B.6.4 Summary of the ex-ante estimation of emission reductions:

Table 10. Total Emission Reductions Total Emission Reductions (tonnes CO2e)

Year

Estimation of project activity

emissions (tCO2e)

Estimation of baseline

emissions (tCO2e)

Estimation of leakage

(tCO2e)

Estimation of overall

emission reductions

(tCO2e) Year1: 2008 - 2009 1,079 7,662 0 6,583 Year2: 2009 - 2010 1,627 11,551 0 9,924 Year3: 2010 - 2011 2,453 17,414 0 14,962 Year4: 2011 - 2012 3,364 26,254 0 22,890 Year5: 2012 - 2013 3,364 26,254 0 22,890 Year6: 2013 - 2014 3,364 26,254 0 22,890 Year7: 2014 - 2015 3,364 26,254 0 22,890

Total (tonnes CO2e) 18,615 141,643 0 123,028

B.7 Application of a monitoring methodology and description of the monitoring plan:

B.7.1 Data and parameters monitored: AES AgriVerde has developed a unique set of data management tools to efficiently capture and report data throughout the project lifecycle. On-site assessment, supplier production data exchange, task tracking, and post-implementation auditing tools have been developed to ensure accurate, consistent, and complete data gathering and project implementation. Tools have also been created to monitor the creation of high quality, permanent ERs using IPCC formulae. By implementing all of these tools, AES AgriVerde enables transparent data collection and verification.


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Data / Parameter: Qy,ww

Data unit: m3

Description: Volume of the wastewater treated in the year “y” Source of data to be used: Data collected on the AES AgriVerde Monitoring Form. Value of data Description of measurement methods and procedures to be applied:

Determined by multiplying the FFB production by the conversion factor for FFB to POME. The conversion factor is verified by a third party on an annual basis.

QA/QC procedures to be applied:

Data used to calculate this parameter will be verified with facility production records and periodic on-site monitoring.

Any comment: Data will be archived electronically and kept for the duration of the project + 2 years.

Data / Parameter: CODy,ww,untreated


Description: Chemical oxygen demand of the wastewater entering the anaerobic treatment/reactor system in the year “y”

Source of data to be used: Data collected on the AES AgriVerde Monitoring Form. Value of data Description of measurement methods and procedures to be applied:

Measured and recorded semi-annually


COD analysis of wastewater samples will be conducted in accordance with equipment manufacturer’s specifications and will include blank and calibration standards.


Data / Parameter: CODy,ww,treated

Data unit: Tonnes/m3 Description: Chemical oxygen demand of the final treated wastewater discharged in the

year “y” Source of data to be used: Data collected on the AES AgriVerde Monitoring Form. Value of data Description of measurement methods and procedures to be applied:

Measured and recorded semi-annually




Data / Parameter: CODy,removed

Data unit: Tonnes/m3 Description: Chemical oxygen demand that is the difference between the inflow COD and

the outflow COD in the year “y”


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Data / Parameter: CODy,removed

Source of data to be used: Data collected on the AES AgriVerde Monitoring Form. Value of data Description of measurement methods and procedures to be applied:

Determined by subtracting CODy,ww,treated from CODy,ww,untreated. Recorded semi-annually.




Data / Parameter: BGPFlare

Data unit: NCM

Description: Amount of biogas recovered and directed to flare for combustion Source of data to be used: Continuous flow meter Value of data Description of measurement methods and procedures to be applied:

Measured and recorded more often than hourly.


AES AgriVerde employs an internal QA audit process that ensures monitoring activities are conducted in accordance with the monitoring plan and verifies the accuracy of data reported.

Any comment: Data will be archived electronically or on paper and kept for the duration of the project + 2 years.

Data / Parameter: MCbiogas

Data unit: Percentage (volume) Description: Methane content of biogas Source of data to be used: Gas analyzer Value of data Description of measurement methods and procedures to be applied:

Measured and recorded periodically. The measuring equipment is calibrated in accordance with the manufacturer specifications. A sufficient number of measurements will be made to meet a 95% confidence level.


Use and calibration of the methane analyzer will be conducted in accordance with manufacturer’s standards. A calibration/service log will be maintained for each methane analyzer.


Data / Parameter: CFEww

Data unit: Percentage Description: Efficiency of flaring process Source of data to be used: Refer to AMS III H, V.9 methodology (paragraph 38, option a) Value of data 0.90* Description of measurement methods and procedures to be applied:

Flares shall be operated in accordance with manufacturer specifications. Flare combustion temperature and biogas flow rate data will be recorded more frequently than hourly.


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Data / Parameter: CFEww

*According to the methodology, “If option (a) is chosen continuous check of compliance with the manufacturers specification of the flare device (temperature, biogas flow rate) should be done. If in any specific hour any of the parameters is out of the range of specifications 50% of default value should be used for this specific hour. For open flare 50% default value should be used, as it is not possible in this case to monitor the efficiency. If at any given time the temperature of the flare is below 500ºC, 0% default value should be used for this period.


All flare monitoring equipment will be operated and calibrated according to manufacturer’s specifications. Flare exhaust temperature and biogas flow data will be compiled and analyzed using software.

Any comment: Electronic flare monitoring data will be stored for the duration of the project + 2 years.

Data / Parameter: PEy,power

Data unit: tCO2e

Description: Emissions from electricity or diesel consumption in the year “y” Source of data to be used: Data collected on the AES AgriVerde Monitoring Form. Value of data Description of measurement methods and procedures to be applied:

Verified and recorded as required. Calculated or measured based upon final implementation of project activity.




Data / Parameter: Sf, end use

Data unit:

Description: End use of final sludge Source of data to be used: Data collected on the AES AgriVerde Monitoring Form. Value of data Description of measurement methods and procedures to be applied:

Verified and recorded as required.


End use of sludge will be monitored and inspected on-site (visually) with verification by mill personnel.



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Data / Parameter: BGPboiler

Data unit: m3 /year Description: Net quantity of biogas combusted in boiler or generator system Source of data to be used: Continuous flow meter Value of data Description of measurement methods and procedures to be applied:

Measured and recorded more often than hourly




Calculation of emission reductions during the crediting period In accordance with the methodology, this type of project (technology option (iv)) requires that “the calculation of emission reductions shall be based on the amount of methane recovered and fuelled or flared, that is monitored ex-post. Also for these cases, the project emissions and leakage will be deducted from the emission reductions calculated from the methane recovered and combusted, except where it can be demonstrated that the technology implemented does not increase the amount of methane produced per unit of COD removed (COD removed is the difference between the inflow COD (CODy,ww,untreated) and outflow COD (CODy,ww,treated)), compared with the technology used in the baseline.24” Inflow and outflow COD is monitored to demonstrate there is no increase in the amount of methane produced per unit of COD removed. Accordingly, emission reductions (ER) during the crediting period will simply be based upon the methane recovered and fueled or flared (My). In addition, as stated in section B.6.1, leakage calculations are not required since the technology being employed in this project is not transferred from or to another activity. The amount of methane recovered or fuelled/flared will be calculated and converted into tonnes of CO2e as follows: Equation 8. Methane recovered and fuelled or flared ex-post

My =BGPFlare *MCbiogas * DCH4,y *CFEww * GWP_CH4 – PEy,power

Where:

My methane recovered and fueled or flared (tCO2e)

BGPFlare amount of biogas recovered and directed to flare for combustion (Nm3).

MCbiogas methane content of biogas (fraction).

24 UNFCCC methodology AMS-III.H (Methane recovery in wastewater treatment), V.9, http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7


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DCH4,y density factor25 of methane (kg/m3)

CFEww efficiency of the flaring process (percentage)

GWP_CH4 global warming potential of methane

PEy,power emissions from electricity or diesel consumption due to the project activity

B.7.2 Description of the monitoring plan:

A monitoring plan has been developed to ensure that accurate and relevant measurements and observations are made to document palm oil mill production metrics, project biogas production and equipment operation, including possible sources of sludge, emissions and leakage. This plan reflects good monitoring practice appropriate to this type of project activity and meets the requirements of the Simplified modalities and procedures for small-scale clean development mechanism project activities.26 Local or in-country personnel are responsible for the collection of all monitoring data. This data is quality checked and then transmitted to AES AgriVerde for secure electronic storage. All data is maintained for a minimum of 2 years beyond the duration of the project.

AES AgriVerde has established a dedicated regional O&M staff to perform activities including, but not limited to, monitoring and collection of parameters, quality audits, personnel training, palm oil mill staff training, and equipment inspections. Separate operations and maintenance manuals have been developed to ensure equipment functions in accordance with required specifications and calibrations. These manuals provide specific guidance to individuals that collect and/or process data. AES AgriVerde staff will perform audits of operations personnel on a regular basis to ensure integrity in the data collection and archiving. An on-site training program will include hands-on proficiency training, question and answer sessions, and an evaluation. Training will be conducted prior to operational start-up. Training topics will include, but are not limited to, CDM project overview, system overview, subsystem specific modules, data collection and quality control, instrument function, malfunction diagnostics, fault reporting and escalation, and facility personnel orientation. Safety and security are elements that will be emphasized in each functional area. Follow-up training will be provided on an as-needed basis. B.8 Date of completion of the application of the baseline and monitoring methodology and the name of the responsible person(s)/entity(ies) The final draft of the application of the methodology was completed on 21/04/2008.

The entity determining the baseline is AES AgriVerde who is the project developer as well as a project participant. Contact information is listed in Annex 1.

25 Normalized to 0 degrees Celsius at 1 ATM and calibrated in NCMH units by the manufacturer. Standard density conversion factors are established by the manufacturer. 26 http://cdm.unfccc.int/Reference/COPMOP/08a01.pdf#page=43


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SECTION C. Duration of the project activity / crediting period C.1 Duration of the project activity: C.1.1. Starting date of the project activity: The starting date for this activity is 04/04/2008. C.1.2. Expected operational lifetime of the project activity: The expected life of this project is 21 years.

C.2 Choice of the crediting period and related information: The project activity will use a renewable crediting period C.2.1. Renewable crediting period C.2.1.1. Starting date of the first crediting period: The starting date of the first crediting period is 01/05/2009 or the project registration date (whichever is latest). C.2.1.2. Length of the first crediting period: The length of the first crediting period is 7y-0m. C.2.2. Fixed crediting period: C.2.2.1. Starting date: C.2.2.2. Length:


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SECTION D. Environmental impacts D.1. If required by the host Party, documentation on the analysis of the environmental impacts of the project activity: In Indonesia, all palm oil mills which process fresh fruit bunches into crude palm oil products (intermediate or final) are governed by specific wastewater regulations27:

• Indonesian Government Regulation No.82/2001 stipulating provisions concerning Water Treatment and Prevention of Water Pollution (Peraturan Pemerintah Republik Indonesia No. 82 tahun 2001 tentang Pengelolaan Kualitas Air dan Pengendalian Pencemaran Air);

• Ministry of Environment Keputusan Menteri Negara Lingkungan Hidup, nomor 28 tahun 2003

tentang Pedoman Teknis Pengkajian Pemanfaatan Air Limbah dari Industri Minyak Sawit pada Tanah Perkebunan Kelapa Sawit

As an extremely polluting effluent with a high organic content, POME discharge is legally regulated to ensure it will not pollute the receiving environment. No discharge of effluent from the mills is permitted without license from the regulatory authority. The regulations do not require specific treatment technologies to ensure the mills adhere to effluent discharge limits. Effluent discharge limits are governed by the following regulations:

• Land application falls under the State Ministry of Environment Decree no. 28/2003 on the Technical Manual of Waste Water application from palm oil industry to palm plantation land.

• Water discharge falls under “Keputusan Menteri Negara Lingkungan Hidup, nomor Kep-

51/MENLH/10/1995 Tentang Baku Mutu Limbah Cair Bagi Kegiatan Industri (the State Ministry of Environment Decree no Kep-51/MENLH/10/1995 on the Wastewater Standard for Industrial Activities).

In addition, mills must comply with relevant policies regarding their impact on the environment. While the national regulation (Ministry of Environment Decree No. 11/2006) does not require methane recovery in wastewater treatment projects to submit an Environmental Impact Assessment (EIA) report, each mill is required submit a six month environmental management and monitoring report to the local Department of Environment (at the district level). Any changes in the wastewater system or performance of the system need to be included in the report. Because the CDM process is quite new to most local DoE offices, a formal meeting with both the mill owner and CDM project developer prior to approving the mill’s “new and improved” wastewater system is often held. In the case of this project site, the head of the local DoE will receive an explanation of the CDM biogas project and its associated benefits as an attachment to the current mill Environmental Management and Monitoring Report. Environment: There are no negative environmental impacts resulting from the proposed project activity. Beyond the principal benefit of mitigating GHG emissions (the primary focus of the proposed project); the proposed activity will also result in positive environmental co-benefits. They include a reduction in 27 http://www.menlh.go.id/archive.php?action=cat&cat=7


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atmospheric emissions of Volatile Organics Compounds (VOCs) that cause odour and acid rain, and promotion of an improved, modernized image of the palm oil production industry. The combination of these factors will make the proposed project site more “neighbour friendly” and environmentally responsible. D.2. If environmental impacts are considered significant by the project participants or the host Party, please provide conclusions and all references to support documentation of an environmental impact assessment undertaken in accordance with the procedures as required by the host Party: No action required.


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SECTION E. Stakeholders’ comments E.1. Brief description how comments by local stakeholders have been invited and compiled: AES AgriVerde invited stakeholders to a meeting to explain both the UNFCCC CDM process and the proposed project activity. This meeting was held on 24/10/2007 at the Hall of PT Sago Nauli Palm Oil Mill Desa Sinunukan, Kecamatan Batahan, Kabupaten Mandailing Natal, Provinsi North Sumatera, Indonesia. Invitations were issued to government officials at the national and local/district levels. Public announcements of the meetings appeared in the following publications:

• Harian Mandiri, 19/10/2007, North Sumatera, Indonesia

All invitations were in the Indonesian Bahasa language. The meeting was attended by project participants, various members from the local community, and producer representatives. A full list of attendees and the meeting minutes are available on request. AES AgriVerde representatives Stefanus Johan gave a presentation addressing the following topics:

• the purpose of the meeting • an overview of global warming and the Kyoto Protocol • UNFCCC CDM processes • project participants, processes and responsibilities • equipment used for evaluation and audits • the information management system • a project example • benefits of the project (environmental and economic) • where to obtain further information • the company’s business role in Indonesia for reducing carbon emissions • the AES AgriVerde partnership with AgCert which has achieved significant regulatory experience

through project work performed at over 1,000 sites. Mr. Ir. Soeyitno, technical advisor for PT Sago Nauli, welcomed the group and stated that this project of PT Sago Nauli and PT AES AgriVerde is indeed beneficial for sustaining our environment. He also stated that the purpose of this meeting is to seek support and share information. Finally, he added that AES AgriVerde has enlightened the community of the importance of current environmental conditions. M. Haposan, Head of Sub-District of Sinunukan, remarked on his hope that this project will have a positive impact on the future, and how renewable energy utilization will help to overcome the energy crisis.


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E.2. Summary of the comments received:

After the presentations, attendees were afforded the opportunity to ask questions regarding the proposed project activities.

Overall, the comments from the attendees at the stakeholders’ meeting were positive and supportive of the project.

E.3. Report on how due account was taken of any comments received: No action required.


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Annex 1

CONTACT INFORMATION ON PARTICIPANTS IN THE PROJECT ACTIVITY

Project Participant Organization: AES AgriVerde Ltd. Street/P.O.Box: 10 Queen Street, Suite 105 Building: Gibbons Building City: Hamilton State/Region: Postfix/ZIP: HM11 Country: Bermuda Telephone: +1 (321) 549-4255 FAX: +1 (321) 722-9008 E-Mail: [email protected] URL: www.aesagriverde.com Represented by: Title: Quality Assurance and Regulatory Director Salutation: Mr. Last Name: Miller Middle Name: A. First Name: Mark Department: Regulatory Mobile: Direct FAX: +1 (321) 722-9008 Direct tel: +1 (321) 549-4255 Personal E-Mail: [email protected]


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Project Participant

Organization: PT AES AgriVerde Indonesia Street/P.O.Box: Suite 25.10, Wisma 46, Kota BNI, JI Jend.Sudirman Kav. 1 Building: City: Jakarta State/Region: Postfix/ZIP: 10220 Country: Indonesia Telephone: +60 21 579 45790 FAX: +60 21 579 45791 E-Mail: URL: www.aesagriverde.com Represented by: Haskarlianus Pasang Title: Country Manager Salutation: Dr. Last Name: Pasang Middle Name: First Name: Haskarlianus Department: Mobile: +62 813 854 8889 Direct FAX: +60 21 579 45791 Direct tel: +60 21 579 45790 Personal E-Mail: Haskarlianus.Pasang @aes.com


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Annex 2

INFORMATION REGARDING PUBLIC FUNDING No public funding is being provided for this project.


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Annex 3

BASELINE INFORMATION

Data available at validation (not presented in Section B.6.2) Description Variable Value Unit Source

Annual FFB production

2008-2009 – 105,063 2009-2010 – 158,392 2010-2011 – 238,791 2011-2015 – 360,000

Tonnes Average based on the most recent years facility records.

Conversion factor of FFB to POME 0.7 Malaysia Department of

Environment28

Volume of wastewater treated in the year “y” Qy,ww

2008-2009 – 73,544 2009-2010 – 110,875 2010-2011 – 167,154 2011-2015 – 252,000

m3

Average calculated based on facility records - Determined

by multiplying the FFB production by the conversion

factor for FFB to POME. Chemical oxygen demand

of the final treated wastewater discharged in

the year “y”

CODy,ww, treated 0.000370 tonnes/m3

Average of successive monthly readings –

independent laboratory test results

Chemical oxygen demand removed by the treatment system “j” of the project activity equipped with

methane recovery in the year “y”

CODy,removed,j 0.031795 tonnes/m3



Chemical oxygen demand removed by the anaerobic

wastewater treatment system “i” in the baseline situation in the year “y”

CODy,removed,i 0.029530 tonnes/m3



Emissions from electricity or diesel consumption in

the year “y” PEy, power 0 tCO2e

In continuity with the baseline scenario, the project will not utilize grid-based electricity.

Since the majority of the electricity used by the facility is produced by the biomass-based boiler(s) for electricity

generation and only a negligible amount of

emissions are from the diesel consumption of the other

generator set(s), it is acceptable to assume that

these project emissions are negligible.

End use of final sludge Sf, enduse Sludge is land applied

Mill records. If sludge is land applied,

PEy,s,final = 0 & MEPy,s,treatment = 0

28 Malaysia Department of Environment publication Industrial Processes & the Environment (Handbook #3) Crude Palm Oil Industry, pp. 23 & 27; http://www.doe.gov.my/index.php?option=com_content&task=view&id=1493&Itemid=761&lang=en


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COD is measured and recorded in *mg/l and is converted to tonnes/m3 COD as follows: mg/L / 1,000,000 = tonnes/m3

**If applicable, project emissions from electricity consumption are estimated based upon the total horsepower (HP) consumed by project activity equipment (converted to kWh). To remain conservative, equipment is assumed to be in operation 24 hours per day, 365 days per year. The following formula is used to convert the data to tCO2e: 29

PEy = (HP * 0.745730 * Hd * Dy * EF) / 1000

Where: PEy Project emissions due to electricity consumption of equipment (tonnes CO2e) HP Horsepower of equipment Hd Hours per day equipment is in use Dy Days per year equipment is in use EF Country specific electricity emission factor Note: Project emissions due to consumption of fossil fuel are determined using the appropriate emission factor for the fuel type(s).

29 http://www.energy-toolbox.vic.gov.au/understanding_your_energy_bill/emission_estimation_methodologies/electricity_emission_estimation_methodologies.html 30 .7457 is the standard scientific conversion factor from horsepower (HP) to Kilowatt Hours (kWh) based on Ohm’s Law


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Annex 4

MONITORING INFORMATION Monitoring: Monitoring activities will be conducted as specified by AMS III.H, Version 9: Methane recovery in wastewater treatment.31

In accordance with the methodology, this type of project (technology option (iv)) requires that “the calculation of emission reductions shall be based on the amount of methane recovered and fuelled or flared, that is monitored ex-post. Also for these cases, the project emissions and leakage will be deducted from the emission reductions calculated from the methane recovered and combusted, except where it can be demonstrated that the technology implemented does not increase the amount of methane produced per unit of COD removed (COD removed is the difference between the inflow COD (CODy,ww,untreated) and outflow COD (CODy,ww,treated)), compared with the technology used in the baseline.32”. The monitoring methodology involves monitoring of the following parameters after project implementation. All sampling and analysis equipment will be operated and calibrated to applicable standards in accordance with manufacturers’ specifications and recommendations. Training will be provided to operations personnel and documented to ensure proper use of monitoring equipment.

For determination of project emissions reductions:

• Total amount of biogas recovered, fuelled or flared will be monitored using in-line flow meters that automatically compensate for temperature and pressure. Readings from the flow meter will be continuously recorded on a data acquisition system and stored electronically in a database.

• The fraction of methane in the gas will be measured periodically at a 95% confidence level using a CH4 gas analyzer. Measurements from the gas analyser will be electronically recorded into a database.

• Chemical oxygen demand (COD) will be measured periodically by collecting samples from the digester influent and effluent (at the digester entrance and exit ports). Samples will be collected and analysed by an independent laboratory and results will be entered into a database.

• The end-use of final sludge exiting the biodigester will be monitored and documented to ensure proper disposition (i.e. soil application).

• The volume of the wastewater treated is determined by multiplying the FFB production by the conversion factor for FFB to POME. The data used to calculate this parameter will be verified with facility production records and periodic on-site monitoring. The conversion factor is verified by a third party on an annual basis.

• Emissions from the consumption of electricity from the grid and/or fossil fuels will be monitored or calculated based on equipment specifications and / or actual fuel consumed based on fuel purchase records.

• Flare parameters are monitored as specified in the Methodology

For determination of flare efficiency:

• Since a 90% default value (Paragraph 38, option (a) of AMS-III.H) will be used, continuous monitoring of compliance with the manufacturer’s specification of the flare device (temperature,

31 UNFCCC methodology AMS-III.H (Methane recovery in wastewater treatment), V.9, http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7 32 UNFCCC methodology AMS-III.H (Methane recovery in wastewater treatment), V.9, http://cdm.unfccc.int/UserManagement/FileStorage/CDMWF_AM_743QMM1YKHH15AK2AZAVAIJHRGD5R7


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biogas flow rate) will be performed. To accomplish this, a thermocouple will be installed on the flare. Measurements from the thermocouple will be electronically recorded into a database.

o If at any time the parameters are out of range of manufacturer specifications, a 50% default value will be used for that time period.

o If at any time the flare is not operational, a flare efficiency default value of 0% will be used for that time period. Not operational is defined as any one of the following:

The flare is not burning.

There is no record of the temperature of the exhaust gas of the flare.

The recorded temperature of the exhaust gas of the flare is less than 500oC.