Table of Content 2. Leachate Treatment Plant Design for the Proposed Phase 3 Development

TABLE OF CONTENT 2. LEACHATE TREATMENT PLANT DESIGN FOR THE PROPOSED PHASE 3 DEVELOPMENT ...... 1

2.1. LEACHATE GENERATION AND CHARACTERISTIC STUDY ...... 2 2.1.1. Leachate Generation ...... 2 2.1.2. Leachate Characteristic ...... 9 2.2. DESIGN BASIS...... 12 2.2.1. Leachate Quantity and Quality ...... 12 2.2.2. Limitation of Leachate Treatment...... 12 2.3. PROCESS DESCRIPTION ...... 13 2.3.1. Raw Leachate ...... 13 2.3.2. Anaerobic Biological Treatment: Anaerobic MBBR Tank ...... 13 2.3.3. Aerobic Biological Treatment: Moving Bed Biofilm Reactor (MBBR) ...... 13 2.3.3.1. Introduction of BioChip™ MBBR ...... 13 2.3.3.2. Introduction to the Moving Bed Biofilm Reactor ...... 14 2.3.4. Aerobic Biological Treatment: Activated Sludge Process (ASP) ...... 16 2.3.5. Biological Clarifier ...... 17 2.3.6. Physical-Chemical Treatment ...... 18 2.3.7. Filtration System ...... 19 2.3.8. Sludge Management ...... 20 2.4. DESIGN CALCULATION ...... 21 2.4.1. Collection Pond ...... 21 2.4.2. Anaerobic MBBR Tank 1 / 2 ...... 21 2.4.3. Primary Clarifier ...... 22 2.4.4. Buffer Tank ...... 22 2.4.5. Moving Bed Biofilm Reactor (MBBR Tank) ...... 22 2.4.6. Activated Sludge Process (ASP) ...... 31 2.4.7. Degassing Tank ...... 35 2.4.8. Biological Clarifier ...... 35 2.4.9. Clarified Water Sump ...... 36 2.4.10. Mixing Tank 1 / 2 (for RED + OXY Mixing to generate Ferrate VI) ...... 36 2.4.11. Flocculation Tank (for ABSORB Mixing) ...... 39 2.4.12. Inclined Plate Clarifier (IPC) ...... 39 2.4.13. Clarified Water Tank ...... 39 2.4.14. Sand Filter ...... 39 2.4.15. Filtered Water Tank ...... 40 2.4.16. Sludge Holding Tank ...... 40 2.4.17. Belt Press ...... 40 2.4.18. Filtrate Sump ...... 41 2.5. MONITORING OF LTP PERFORMANCE ...... 42

2.6. DESIGN DRAWINGS ...... 44

2.7. TECHNICAL SPECIFICATION AND SCOPE OF SUPPLY ...... 45 2.7.1. Tanks / RC and Structural Works Specifications ...... 45 2.7.2. FRP / HDPE Tanks Specification ...... 46 2.7.3. Equipment Specification ...... 46

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang

LIST OF FIGURE Figure 2.1-1 Leachate Generation Mass Balance Diagram ...... 2 Figure 2.1-2 Leachate Generation (M3/Day) Over Time Duration ...... 6 Figure 2.1-3 Leachate Generation Areas (Landfill Areas) Of Phase 1 & 2 ...... 7 Figure 2.1-4 Leachate Collection System For The Pulau Burung Sanitary Landfill 8 Figure 2.3-1 Retaining Screen and SS perforated air pipe in MBBR Tank ...... 14 Figure 2.3-2 BioChip after 4 weeks of operation ...... 15 Figure 2.3-3 BioChip after 16 weeks of operation ...... 15 Figure 2.3-4 Air distribution pipe from air blower to air diffusers inside the ASP Tank ...... 17 Figure 2.3-5 Surface aerator in the ASP to ensure there is enough oxygen for biological degradation ...... 17 Figure 2.3-6 Biological Clarifier with Mechanical Scrapping System ...... 18 Figure 2.3-7 Inclined Plate Clarifier ...... 18 Figure 2.3-8 Auto Polymer Preparation ...... 20 Figure 2.3-9 Belt Press with polymer conditioning tank, drum thickener and squeezing rolls for drier sludge cake ...... 20 Figure 2.3-10 Sludge cake generated from the Belt Press ...... 20

LIST OF TABLE Table 2.1-1 Leachate Generation Computation ...... 4 Table 2.1-2 Leachate Effluent Characteristics Study ...... 10 Table 2.1-3 Parameters Required For Treatment ...... 11

LIST OF APPENDICES Appendix 2-1 Sampling Location of the Leachate Appendix 2-2 Scientific Publications of Ferrate Vi Treatment Appendix 2-3 RED-OXY + ABSORB (Ferrate VI) Supplier Technical Info Appendix 2-4 Engineering Design Drawings Appendix 2-5 Guidelines of Special Management of Scheduled Wastes

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang

2. Leachate Treatment Plant Design for the Proposed Phase 3 Development

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-1

2.1. Leachate Generation and Characteristic Study

2.1.1. Leachate Generation

A comprehensive leachate generation projection study has been conducted to quantify the leachate quantity to be fed into the proposed Leachate Treatment Plant (LTP).

Figure 2.1-1 depicts in a simplified leachate generation diagram for the proposed LTP. From the figure, it may be noted there are actually 4 sources of leachate influent which shall be fed into the LTP for treatment to meet the permissible discharge limits for the treated effluent stipulated in the Schedule II of the Environmental Quality (Control of Pollution from Solid Waste Transfer Station & Landfill) Regulations 2009, made under the Environmental Quality Act 1974.

The leachate sources are basically:

1) Phase 3 Landfill Cells (Cell 1 to Cell 6) 2) Phase 1 & 2 Landfill Areas (Area I to Area VI) 3) MRF Plant (with throughput capacity of 2,000 tonne per day or 2,000TPD) 4) Phase 1 & 2 Ditches (filled with leachate undergone recirculation process during Phase 1 & 2 landfill operation – estimated volume at 370,000m3)

However, it must be noted only leachate (or wastewater) sources from Phase 3 Landfill Cells, Phase 1 & 2 Landfill Areas and MRF Plant are long-term sources. Phase 1 & 2 perimeter ditches containment of leachate shall be emptied after the leachate has been drawn out, and shall be regarded as short-term source.

Figure 2.1-1 Leachate Generation Mass Balance Diagram

For the purpose of computation of the leachate generation with landfill cells (Phase 3 new cells) and existing landfill (Phase 1 & Phase 2 landfill areas), a rational equation method, developed based on rainfall intensity has been employed for this study, as follows:-

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-2

It may be noted the rainfall intensity to be determined in the rational equation method shall be a daily flow rate, and has been quantified as 5.71mm/day (or 10 year annual return rainfall intensity of 136.96mm over 24 hours period).

As for the leachate coefficient, C, the value is unitless and shall be between 0 to 1. The following C values have been employed for the leachate computation for various life cycle of the landfill cells or landfill areas:

1) Active operational landfill cell, C = 0.5 2) Newly fully filled landfill cell (less than 5 years), C = 0.4 3) Newly closed landfill cell (less than 5 years), C = 0.3 4) Fully closed land fil cell (more than 5 years), C = 0.2

The outcome of the leachate generation computation is as included in Table 2.1-1.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-3

Table 2.1-1 Leachate Generation Computation

Year 42 Onwards (Post DURATION Year 0 - 5 Year 5 - 11 Year 11 - 16 Year 16 - 22 Year 22 - 30 Year 30 - 37 Year 37 - 42 (Post Closure) Closure)

Sub

Sub

Area (Acres) Area

Q (m3/day) Q (m3/day) Q Q (m3/day) Q (m3/day) Q (m3/day) Q (m3/day) Q (m3/day) Q

C, Leachate Leachate C, Leachate C, Leachate C, Leachate C, Leachate C, Leachate C, Leachate C, Leachate C,

I (mm/day)

Coefficient Coefficient Coefficient Coefficient Coefficient Coefficient Coefficient Coefficie

Area (m2) Area

(m3/day) (m3/day) (m3/day) (m3/day) (m3/day) (m3/day) (m3/day) (m3/day)

-

Cell No.Cell

Q Q Q Q Q Q Q Q

(m3/day)

-

Catchment

Area (m2) Area

------

Total Total Total Total Total Total Total Total

nt

1 32 129500 1 - 1 51800 5.71 0.5 147.803 147.803 0.4 118.242 118.242 0.3 88.682 88.682 0.2 59.121 59.121 0.2 59.121 59.121 0.2 59.121 59.121 0.2 59.121 59.121 0.2 59.121 59.121

1 - 2 38850 5.71 0.5 110.852 258.655 0.4 88.682 206.924 0.3 66.511 155.193 0.2 44.341 103.462 0.2 44.341 103.462 0.2 44.341 103.462 0.2 44.341 103.462 0.2 44.341 103.462 1 - 3 38850 5.71 0.5 110.852 369.507 0.4 88.682 295.605 0.3 66.511 221.704 0.2 44.341 147.803 0.2 44.341 147.803 0.2 44.341 147.803 0.2 44.341 147.803 0.2 44.341 147.803 2 32 129500 2 - 1 43167 5.71 0 0.000 369.507 0.5 123.169 418.774 0.4 98.535 320.239 0.3 73.901 221.704 0.2 49.268 197.070 0.2 49.268 197.070 0.2 49.268 197.070 0.2 49.268 197.070 2 - 2 43167 5.71 0 0.000 369.507 0.5 123.169 541.943 0.4 98.535 418.774 0.3 73.901 295.605 0.2 49.268 246.338 0.2 49.268 246.338 0.2 49.268 246.338 0.2 49.268 246.338 2 - 3 43167 5.71 0 0.000 369.507 0.5 123.169 665.112 0.4 98.535 517.309 0.3 73.901 369.507 0.2 49.268 295.605 0.2 49.268 295.605 0.2 49.268 295.605 0.2 49.268 295.605 3 32 129500 3 - 1 38850 5.71 0 0.000 369.507 0 0.000 665.112 0.5 110.852 628.161 0.4 88.682 458.188 0.3 66.511 362.117 0.2 44.341 339.946 0.2 44.341 339.946 0.2 44.341 339.946 3 - 2 42735 5.71 0 0.000 369.507 0 0.000 665.112 0.5 121.937 750.099 0.4 97.550 555.738 0.3 73.162 435.279 0.2 48.775 388.721 0.2 48.775 388.721 0.2 48.775 388.721 3 - 3 47915 5.71 0 0.000 369.507 0 0.000 665.112 0.5 136.717 886.816 0.4 109.374 665.112 0.3 82.030 517.309 0.2 54.687 443.408 0.2 54.687 443.408 0.2 54.687 443.408 4 32 129500 4 - 1 43167 5.71 0 0.000 369.507 0 0.000 665.112 0 0.000 886.816 0.5 123.169 788.281 0.4 98.535 615.844 0.3 73.901 517.309 0.2 49.268 492.676 0.2 49.268 492.676 4 - 2 43167 5.71 0 0.000 369.507 0 0.000 665.112 0 0.000 886.816 0.5 123.169 911.450 0.4 98.535 714.380 0.3 73.901 591.211 0.2 49.268 541.943 0.2 49.268 541.943

LEACHATEFROM PHASE LANDFILL 3 4 - 3 43167 5.71 0 0.000 369.507 0 0.000 665.112 0 0.000 886.816 0.5 123.169 1034.619 0.4 98.535 812.915 0.3 73.901 665.112 0.2 49.268 591.211 0.2 49.268 591.211 5 45 182100 5 - 1 54630 5.71 0 0.000 369.507 0 0.000 665.112 0 0.000 886.816 0 0.000 1034.619 0.5 155.878 968.792 0.4 124.702 789.814 0.3 93.527 684.737 0.2 62.351 653.562 5 - 2 60093 5.71 0 0.000 369.507 0 0.000 665.112 0 0.000 886.816 0 0.000 1034.619 0.5 171.465 1140.258 0.4 137.172 926.986 0.3 102.879 787.616 0.2 68.586 722.148 5 - 3 67377 5.71 0 0.000 369.507 0 0.000 665.112 0 0.000 886.816 0 0.000 1034.619 0.5 192.249 1332.507 0.4 153.799 1080.786 0.3 115.349 902.966 0.2 76.900 799.047 6 32 129500 6 - 1 43167 5.71 0 0.000 369.507 0 0.000 665.112 0 0.000 886.816 0 0.000 1034.619 0 0.000 1332.507 0.5 123.169 1203.954 0.4 98.535 1001.501 0.3 73.901 872.949 6 - 2 43167 5.71 0 0.000 369.507 0 0.000 665.112 0 0.000 886.816 0 0.000 1034.619 0 0.000 1332.507 0.5 123.169 1327.123 0.4 98.535 1100.036 0.3 73.901 946.850 6 - 3 43167 5.71 0 0.000 369.507 0 0.000 665.112 0 0.000 886.816 0 0.000 1034.619 0 0.000 1332.507 0.5 123.169 1450.292 0.4 98.535 1198.571 0.3 73.901 1020.751

Sub

Sub

Area (Acres) Area

Q (m3/day) Q (m3/day) Q (m3/day) Q (m3/day) Q (m3/day) Q (m3/day) Q (m3/day) Q (m3/day) Q

C, Leachate Leachate C, Leachate C, Leachate C, Leachate C, Leachate C, Leachate C, Leach C, Leachate C,

I (mm/day)

Coefficient Coefficient Coefficient Coefficient Coefficient Coefficient Coefficient Coefficient

Area (m2) Area

(m3/day) (m3/day) (m3/day) (m3/day) (m3/day) (m3/day) (m3/day) (m3/day)

Area No.Area

-

Q Q Q Q Q Q Q Q

-

Catchment

Area (m2) Area

------

Total Total Total Total Total Total Total Total

ate

I 6.4 25900 I 25900 5.71 0.2 29.561 29.561 0.2 29.561 29.561 0.2 29.561 29.561 0.2 29.561 29.561 0.2 29.561 29.561 0.2 29.561 29.561 0.2 29.561 29.561 0.2 29.561 29.561 II 12.99 52600 II-A 26300 5.71 0.5 75.043 104.603 0.4 60.034 89.595 0.3 45.026 74.586 0.2 30.017 59.578 0.2 30.017 59.578 0.2 30.017 59.578 0.2 30.017 59.578 0.2 30.017 59.578 II-B 26300 5.71 0.2 30.017 134.620 0.2 30.017 119.612 0.2 30.017 104.603 0.2 30.017 89.595 0.2 30.017 89.595 0.2 30.017 89.595 0.2 30.017 89.595 0.2 30.017 89.595 III 18.62 75400 III-A 37700 5.71 0.5 107.571 242.191 0.4 86.057 205.668 0.3 64.542 169.146 0.2 43.028 132.623 0.2 43.028 132.623 0.2 43.028 132.623 0.2 43.028 132.623 0.2 43.028 132.623 III-B 37700 5.71 0.2 43.028 285.219 0.2 43.028 248.697 0.2 43.028 212.174 0.2 43.028 175.651 0.2 43.028 175.651 0.2 43.028 175.651 0.2 43.028 175.651 0.2 43.028 175.651 IV 7.34 29700 IV 29700 5.71 0.2 33.898 319.117 0.2 33.898 282.594 0.2 33.898 246.071 0.2 33.898 209.549 0.2 33.898 209.549 0.2 33.898 209.549 0.2 33.898 209.549 0.2 33.898 209.549 V 17.23 69700 V 69700 5.71 0.2 79.551 398.668 0.2 79.551 362.145 0.2 79.551 325.622 0.2 79.551 289.100 0.2 79.551 289.100 0.2 79.551 289.100 0.2 79.551 289.100 0.2 79.551 289.100

LEACHATEFROM PHASE 1 & 2 LANDFILL VI 3.92 15900 VI 15900 5.71 0 0.000 398.668 0 0.000 362.145 0 0.000 325.622 0 0.000 289.100 0 0.000 289.100 0 0.000 289.100 0 0.000 289.100 0 0.000 289.100

TOTAL LEACHATE FROM LANDFILL 768.174 1027.257 1212.438 1323.718 1621.606 1739.392 1487.671 1309.851

LEACHATE FROM MRF PLANT 100.000 100.000 100.000 100.000 100.000 100.000 100.000 100.000

TOTAL LEACHATE FROM LANDFILL + MRF 868.174 1127.257 1312.438 1423.718 1721.606 1839.392 1587.671 1409.851 PLANT

LEACHATE FROM

DITCHES 370,000

CAPACITY AVAILABLE FOR TREATMENT OF LEACHATE 1131.82

FROM DITCHES 6

NUMBER OF DAYS FOR EMPTYING 327 LEACHATE IN DITCHES

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-4

From the table, it must be noted that the leachate generation from the Phase 3 landfill cells shall start from 369.5 m3/day during the initial 5 year of operation (Cell 1 operation), and reaches its maximum in year 30-37 period (Cell 6 operation) at 1,450.2 m3/day. While Phase 1 & 2 landfill areas shall decrease from the corresponding durations as above from 398.7 m3/day to 289.1 m3/day. As for the MRF operation, it is estimated each tonne of municipal solid waste (MSW) fed through the MRF recycling system shall yield 50kg of wastewater (or leachate), hence 2,000 tonne of MSW at maximum plant operational capacity shall yield 2,000 x 50 kg = 100,000kg or 100 tonne of wastewater (or leachate).

Total leachate collected from the 3 long-term leachate sources as above shall be from 868.2 m3/day in the initial 5 year duration, and increases to 1,839.4 m3/day in the year 30-37 duration.

Therefore, it is sufficient to design and construct an LTP of 2,000m3/day treatment capacity to deal with the leachate generated from the operation of Pulau Burung Sanitary Landfill. This capacity has about 8% safety buffer, and shall consider as adequate. This is due to the fact that the Phase 3 landfill cells (future cells to be constructed) have a minimum of 1 – 2m of inverted containment for temporary leachate collection, and hence the rainfall and biodegradation generated leachate will not be flowed out from the landfill cells immediately, and has a significant detention time before finding its way into the leachate collection and conveyance system. Furthermore, there is a contingency measure whereas the generated leachate from all the sources shall flow into a raw leachate pond, with an estimated capacity of 60,000m3 (30 day raw leachate storage), and this shall further provide buffer for contingency in the event of exceptional high rainfall intensity, or in the event of failure of the LTP to treat the leachate to meet the Schedule II discharge standards.

During the first year of LTP operation, after taking into the three (3) long-term leachate sources as above, the balance capacity in the LTP for daily treatment is about 1,131.8 m3/day. Hence, if we feed the leachate Phase 1 & 2 recirculation ditches into the LTP, it will take 327 days, or about 11 months to completely empty or draw out the leachate, based on a preliminary quantity of 370,000m3 of total leachate.

Figure 2.1-2 shows the fluctuation trend of leachate generation over the life cycle of the landfill. The may be noted except from year 1 operation when leachate from Phase 1 & 2 ditches is being drawn out, leachate generated shall not expect to exceed 2,000 m3/day.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-5

Figure 2.1-2 Leachate Generation (M3/Day) Over Time Duration

(m3)

Figure 2.1–3 depicts the leachate generation areas (landfill areas) of Phase 1 & 2, with most areas being closed from landfilling activities, with only less than 50% of the Area II and Area III in still in active utilisation. But all landfilling activities at Phase 1 & 2 shall cease once Cell 1 of Phase 3 (an advance cell construction) ready for operation.

Figure 2.1–4 depicts the leachate collection system for the Pulau Burung Sanitary Landfill, with the overall Phase 3 landfill cells shall have 3 sub-catchments each to facilitate leachate collection.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-6

Figure 2.1-3 Leachate Generation Areas (Landfill Areas) Of Phase 1 & 2

DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-7

Figure 2.1-4 Leachate Collection System For The Pulau Burung Sanitary Landfill

DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-8

2.1.2. Leachate Characteristic

The LTP will be designed to meet second schedule of leachate discharge standard as per the Environmental Quality (Control of Pollution from Solid Waste Transfer Station and Landfill Regulations) 2009. The raw leachate effluent quality from the existing Pulau Burung landfill operation has been monitored and sampled as a basis for prediction of leachate characteristics.

In compliance with the DOE requirement on conducting leachate effluent characteristics study, a 3-day sampling exercise has been planned samples collected at various locations where leachate has been generated and/or leached out. The sampling locations of the leachate has been included in Appendix 2-1.

The 3-days results for the samples collected at various locations during rainy or wet weather conditions, with different generated volume at designated sources have been measured. The recorded data shall be used in the computation exercise to arrive to the projected leachate quality (or leachate characteristics), which shall be employed to develop the LTP design basis. The outcome of the computation (projection) for the leachate characteristics is tabulated in Table 2.1-2.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-9

Table 2.1-2 Leachate Effluent Characteristics Study

LEACHATE SAMPLING & ANALYSIS EXERCISE (BASED ON 3 -DAY LEACHATE CHARACTERISTICS STUDY) LEACHATE CHARACTERISTICS ESTIMATION COMPUTATION

PARAMETERS 16/11/2016 17/11/2016 18/11/2016 3-DAY AVERAGE Leachate Source (Stream) - Rainy Day Scenario

Requirement

Compliance Compliance

Schedule II Schedule

Phase 3 Landfill Phase

MRF Operation Operation MRF Discharge

Leachate from Leachate from Leachate from Leachate from Leachate from Leachate

TEMPORARY TEMPORARY TEMPORARY TEMPORARY TEMPORARY

Active Areas Active

DITCH TPPB DITCH TPPB DITCH TPPB DITCH TPPB DITCH

POND TPPB POND TPPB POND TPPB POND TPPB POND P TPPB POND TPPB POND TPPB POND 21 & Phase 21 & Phase

Parameters

LEACHATES LEACHATES LEACHATES LEACHATES LEACHATES LEACHATES LEACHATES LEACHATES LEACHATES LEACHATES LEACHATES LEACHATES (Composite

Compacted Compacted

All Sources Sources All

LEACHATE LEACHATE

Perimeter Perimeter

Source 1 : Source 2 : Source S 4 : Source

LANDFILL LANDFILL LANDFILL LANDFILL LANDFILL

(Phase 3) (Phase 5: Source

OND TPPB

Sample)

ource 3 : ource

Tipped Tipped

Areas

MSW

TPPB TPPB TPPB TPPB

Cells

Quantity 50 60 290 100 1500 2000 - - (m3/day) Percentage (%) 2.5% 3.0% 14.5% 5.0% 75.0% 100.0% - - Combined Wastewater S1 S2 S3 S4 Projected Leachate - - Parameter: (Design) Temperature, oC 36.4 33.7 37.4 37.2 29.24 31.96 35.22 35.93 31.46 28.92 32.01 33.81 32.37 31.52 34.86 35.63 35.63 34.86 31.52 32.37 32.50 - Temperature, oC 40 pH value 8.15 7.68 7.42 7.24 8.22 7.75 7.55 7.39 8.15 7.79 7.31 7.33 8.17 7.74 7.43 7.32 7.32 7.43 7.74 8.17 7.75 - pH value 6.9-9.0 B.O.D, mg/l B.O.D, mg/l (5days 417 11850 16860 27450 568 7470 20820 27420 462 5520 23340 23700 482 8280 20340 26190 26190 20340 8280 482 9959 10000 20 (5days @ 20 oC) @ 20 oC) C.O.D, mg/l 1186 12201 24008 40409 1215 10967 27960 32604 1346 6336 25641 27126 1249 9835 25870 33380 33380 25870 9835 1249 12396 15000 C.O.D, mg/l 400 Suspended solid, Suspended solid, 130 625 725 1020 90 1350 790 815 106 385 920 800 109 787 812 878 878 812 787 109 663 1000 50 mg/l mg/l nd nd nd nd nd nd nd nd nd nd nd nd nd nd nd nd nd nd nd Mercury, mg/l nd (<0.005) nd (<0.005) - Mercury, mg/l 0.005 (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) (<0.005) nd nd Cadmium, mg/l nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) nd (<0.01) - Cadmium, mg/l 0.01 (<0.01) (<0.01) nd nd Chromium+6, mg/l nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) - Chromium+6, mg/l 0.05 (<0.05) (<0.05) nd Arsenic, mg/l 0.05 nd (<0.05) 0.07 nd (<0.05) nd (<0.05) 0.05 0.05 nd (<0.05) nd (<0.05) 0.05 0.05 nd (<0.05) nd (<0.05) 0.05 0.057 0.06 0.05 nd (<0.05) nd (<0.05) nd (<0.05) - Arsenic, mg/l 0.05 (<0.05) nd nd Cyanide, mg/l nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) nd (<0.05) - Cyanide, mg/l 0.05 (<0.05) (<0.05) nd nd Lead, mg/l 0.1 0.1 nd (<0.1) 0.1 nd (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) 0.1 nd (<0.1) 0.1 0.1 0.1 0.10 0.10 0.10 nd (<0.1) 0.10 - Lead, mg/l 0.1 (<0.1) (<0.1) Chromium+3, mg/l 0.06 0.14 0.12 0.20 0.07 0.1 0.14 0.17 0.08 0.08 0.16 0.17 0.07 0.11 0.14 0.18 0.18 0.14 0.11 0.07 0.11 - Chromium+3, mg/l 0.2 nd Copper, mg/l 0.3 0.2 0.5 nd (<0.2) 0.2 0.3 0.5 nd (<0.2) nd (<0.2) 0.4 0.4 nd (<0.2) 0.3 0.3 0.5 0.47 0.30 0.25 nd (<0.2) 0.34 0.5 Copper, mg/l 0.2 (<0.2) Manganese, mg/l 0.3 3.9 2.0 6.2 0.3 1.6 4.5 5.7 0.3 1.2 5.3 5.4 0.3 2.2 3.9 5.8 5.77 3.93 2.23 0.30 2.40 5.0 Manganese, mg/l 0.2 nd Nickel, mg/l 0.2 nd (<0.2) 0.3 nd (<0.2) 0.2 0.2 0.2 nd (<0.2) nd (<0.2) 0.2 0.2 nd (<0.2) 0.2 0.2 0.2 0.23 0.20 0.20 nd (<0.2) 0.21 - Nickel, mg/l 0.2 (<0.2) nd nd Tin, mg/l nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) nd (<0.2) - Tin, mg/l 0.2 (<0.2) (<0.2) nd Zinc, mg/l 1.2 1.2 1.8 nd (<0.2) 1 1.1 1.4 nd (<0.2) 0.5 1.4 1.6 nd (<0.2) 0.9 1.2 1.6 1.60 1.23 0.90 nd (<0.2) 1.24 - Zinc, mg/l 2.0 (<0.2) Boron, mg/l 3.1 7.5 5.8 10.3 3.5 5.6 8.1 9.8 3.5 5.1 8.1 8.3 3.4 6.1 7.3 9.5 9.47 7.33 6.07 3.37 6.02 10.0 Boron, mg/l 1.0

Iron, mg/l 7.2 52.3 39.8 64.8 8.2 61.4 73.7 100.2 9.3 12.9 73.4 88.5 8.2 42.2 62.3 84.5 84.50 62.30 42.20 8.23 42.05 100.0 Iron, mg/l 5.0

Phenol, mg/l 0.315 0.501 0.375 0.423 0.306 0.459 0.291 0.291 0.291 0.369 0.564 0.304 0.304 0.443 0.410 0.339 0.34 0.41 0.44 0.30 0.40 1.000 Phenol, mg/l 0.001 Free Chlorine, nd nd nd (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) n.d (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) n.d (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) n.d (<0.1) nd (<0.1) n.d (<0.1) - Free Chlorine, mg/l 2.0 mg/l (<0.1) (<0.1) Sulphide, mg/l 0.5 1.2 4.5 3.6 0.1 1.5 1.7 1.1 0.1 2 2.4 1.4 0.2 1.6 2.9 2.0 2.03 2.87 1.57 0.23 1.50 5.0 Sulphide, mg/l 0.5 Oil & Grease, 8 28 18 32 6.0 14 16 36 14 16 26 28 9 19 20 32 32.00 20.00 19.33 9.33 18.68 50.0 Oil & Grease, mg/l 5.0 mg/l nd nd Silver, mg/L nd (<0.1) nd (<0.1) 0.1 nd (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) n.d (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) n.d (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) nd (<0.1) n.d (<0.1) nd (<0.1) n.d (<0.1) - Silver, mg/L 0.1 (<0.1) (<0.1) Aluminium, mg/L 2.6 3.6 32.2 3.6 2.2 46.3 4.8 2.4 1.7 7.4 2.2 1.9 2.2 19.1 13.1 2.6 2.63 13.07 19.10 2.17 13.34 - Aluminium, mg/L 15.0

nd nd Selenium, mg/L nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) nd (<0.02) - Selenium, mg/L 0.02 (<0.02) (<0.02) nd Barium, mg/L 0.4 0.4 0.7 nd (<0.2) 0.3 0.4 0.6 nd (<0.2) 0.2 0.6 0.6 nd (<0.2) 0.3 0.5 0.6 0.63 0.47 0.30 nd (<0.2) 0.47 - Barium, mg/L 1.0 (<0.2) Fluoride, mg/L 4.5 6.5 16.6 5.3 3.8 4.1 4.8 7.0 1.9 4.6 5.1 5.0 3.4 5.1 8.8 5.8 5.77 8.83 5.07 3.40 5.26 10.0 Fluoride, mg/L 2.0

Formaldehyde, Formaldehyde, 0.8 5.8 2.5 3.8 1.0 2.6 3.6 3.4 0.7 3.6 3.2 2.7 0.8 4.0 3.1 3.3 3.30 3.10 4.00 0.83 3.19 5.0 1.0 mg/L mg/L Ammonical Ammonical 195.4 902.0 1103.2 1755.3 201.1 861.8 1815.6 1453.6 208.6 731.7 1709.2 1720.7 201.7 831.8 1542.7 1643.2 1643.20 1542.67 831.83 201.70 872.24 1500.0 5.0 Nitrogen, mg/L Nitrogen, mg/L Colour, ADMI pH Colour, ADMI pH >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 3000.0 100.0 (as is) (as is) Colour, ADMI pH Colour, ADMI pH >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 >500 3000.0 100.0 (7.0) (7.0)

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-10

It must be noted there are 4 sources where the 3-day composite samples (daytime and noontime) have been collected in order to resemble the leachate quality of the future Pulau Burung Sanitary Landfill when the proposed 2,000m3 treatment capacity LTP to be in operation.

These sample sources are: 1) Source 1 : Leachate from Tipped Compacted MSW – leachate generated from fresh MSW tipped from compactor trucks or haulage trucks – quantified at 50m3 on a wet day of operation 2) Source 2 : Leachate from Active Landfill Area (on daily operation) in Area III – leachate generated from Phase 1 & 2 newly compacted landfill layer – quantified at 60m3 on a wet day of operation 3) Source 3 : Leachate from perimeter areas (ditches or dykes) around Phase 1 & 2 landfill – leachate from ceased landfill areas – quantified at 290 m3 on a wet day of operation 4) Source 4 : Leachate collected at an existing raw leachate pond – leachate generated from some recycling activities on incoming MSW at the Phase 1 & 2 recycling facilities – the quality of the leachate shall resemble future MRF plant leachate/wastewater characteristics quantified at 100m3 5) Source 5 : Leachate from future Phase 3 landfill cells (Cell 1 to Cell 6) – there is no sample may be collected from these cells – the quantity expected to be 1,500m3, and the quality of the characteristics shall be average of the Source 1, Source 2, Source 3 and Source 4 combined, and quantified as the determinant quality for leachate characteristics design of the LTP

Table 2.1-3 below summarises the computed leachate characteristics used for the LTP design team to consider for design engineering. Out of the 29 parameters listed under the Schedule II (Regulation 13), fifteen (15) parameters on the raw leachate from combined sources are projected to have exceeded the threshold limits allowed under the Schedule II requirements. Overall projected raw leachate quality and treated leachate quality shall be submitted later to DOE as part of Written Notification requirements.

Table 2.1-3 Parameters Required For Treatment SCHEDULE II RAW LEACHATE QUALITY PARAMETERS COMPLIANCE (COMPOSITE) REQUIREMENT* Quantity (m3/day) 2000 - Percentage (%) 100.0% - Wastewater Parameter: Combined Leachate (Design) - B.O.D, mg/l (5days @ 20 oC) 10000 20 C.O.D, mg/L 15000 400 Suspended solid, mg/L 1000 50 Copper, mg/L 0.5 0.2 Manganese, mg/L 5.0 0.2 Boron, mg/L 10.0 1.0 Iron, mg/L 100.0 5.0 Phenol, mg/L 1.0 0.001 Sulphide, mg/L 5.0 0.5 Oil & Grease, mg/L 50.0 5.0 Fluoride, mg/L 10.0 2.0 Formaldehyde, mg/L 5.0 1.0 Ammonical Nitrogen, mg/L 1500.0 5.0 Colour, ADMI pH (as is) 3000.0 100.0 Colour, ADMI pH (7.0) 3000.0 100.0

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-11

2.2. Design Basis

2.2.1. Leachate Quantity and Quality

Leachate Quantity

Flowrate Capacity : 2,000 m³/day Design Capacity : 83.33 m³/hr @ 24 hours Overall LTP Operation Hours : 24 hours

Leachate Quality

PARAMETER Peak Load Treated Effluent B.O.D, mg/l (5days @ ≤ 10,000 ≤ 20 20 oC) C.O.D, mg/l ≤ 15,000 ≤ 400 Suspended solid, mg/l ≤ 1,000 ≤ 50 Ammonical Nitrogen, ≤ 1,500.0 ≤ 5.0 mg/L Oil & Grease, mg/L ≤ 50.0 ≤ 5.0 Copper, mg/L ≤ 0.5 ≤ 0.2 Manganese, mg/L ≤ 5.0 ≤ 0.2 Boron, mg/L ≤ 10.0 ≤ 1.0 Iron, mg/L ≤ 100.0 ≤ 5.0 Phenol, mg/L ≤ 1.0 ≤ 0.001 Sulphide, mg/L ≤ 5.0 ≤ 0.5 Fluoride, mg/L ≤ 10.0 ≤ 2.0 Formaldehyde, mg/L ≤ 5.0 ≤ 1.0 Colour, ADMI pH (as ≤ 3,000.0 ≤ 100.0 is) Colour, ADMI pH (7.0) ≤ 3,000.0 ≤ 100.0

Note: a. The leachate (particular COD parameter) must be biodegradable so the treated water can meet the final discharge water quality as stipulated. b. The leachate shall not be toxic that impede the growth of bacteria in the biological plant.

2.2.2. Limitation of Leachate Treatment

Note: Leachate from the following sources if any, shall NOT be mixed with the raw leachate from the factory production process.

a) Storm water b) Septic tank c) Canteen waste d) Cooling tower e) Regen Wastewater f) Lab Wastewater g) RO reject water

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-12

2.3. PROCESS DESCRIPTION

2.3.1. Raw Leachate

a) Raw leachate will be flow into Collection Pond. Surface Aerator will be installed to keep the leachate in the pond aerated to improve leachate treatability in following treatment system.

b) The effluent will be flow to a Screen Channel where solid particles will be screened off before entering the Oil Trap & Oil Sump.

c) Oil Trap & Oil Sump are used to remove the excessive oil & grease found in the leachate. The de-oiled effluent will be flow to a Pump Sump before pump for further treatment.

2.3.2. Anaerobic Biological Treatment: Anaerobic MBBR Tank

a) Leachate will be pumped to Anaerobic Biological Treatment. Bio-carrier is loaded in the Anaerobic MBBR Tank, which these bio-carrier are mixed mechanically with mixer.

b) Leachate from the Anaerobic MBBR Tank will then be overflowed to Primary Clarifier and Buffer Tank before the effluent is pumped to MBBR Tank for further biological Treatment.

c) In the Primary Clarifier, the sludge will settle at the bottom of the clarifier while the supernatant overflows to the anaerobic biological treatment.

d) Sludge collected at the bottom of the hopper will periodically be recirculated back to the Anaerobic MBBR Tank.

2.3.3. Aerobic Biological Treatment: Moving Bed Biofilm Reactor (MBBR)

a) The effluent from Buffer Tank will pumped to MBBR Tank for biological treatment. The detail of MBBR process is further described at 2.3.1 and 2.3.2.

b) The biological treated leachate from MBBR tank shall overflow from ASP Tank to Biological Clarifier for further biological polishing. Then the treated leachate shall channel for further Physical-Chemical Treatment process.

2.3.3.1. Introduction of BioChip™ MBBR

The BioChip™ MBBR serves for biological treatment of highly loaded industrial and municipal leachate. The treatment process is an aerobic and/or anaerobic operating at high volume loads, allowing the reactors and basins to be much smaller than conventional plants and thus reducing the cost.

The BioChip™ MBBR supplies a protected surface of approximate 3,000 m2/m3. The micro- organisms on the BioChip are protected in the pores and the open surface is cleaned by the shear-force during moving and attrition to each other. Slime, sludge and other deposits of materials inside of carriers are not favourable for the growth of the micro-organism. Therefore, the self-cleaning with the shear force is one of the advantages of the BioChip™ MBBR.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-13

The BioChip™ MBBR carrier are not only used in new plants, they can be used also for the upgrading of existing activated sludge processes. The biofilm process can be used as stand- alone process, in combination with preliminary treatment steps and in final polishing stages.

The parabolic benefits in easy and active moving of the carrier and prevents clogging in retention areas. The carriers are suspended and in continuous movement in the bioreactor.

Advantages of using Bio-Media:- a. Lower reaction volume required; b. Lowest energy requirement; c. Extendable performance rate; d. Highest safety in operation.

2.3.3.2. Introduction to the Moving Bed Biofilm Reactor

The Moving Bed Biofilm Reactor (MBBR) is a biofilm variation of the activated sludge leachate treatment process. In the MBBR process, the bio-film grows on bio-carriers freely suspended in the mixed liquor of the reactor (basin). Bio-carrier movement within the reactor is produced by an engineered aeration system. Retaining screen (referred to as sieves) keep the bio-carriers in the reactor.

Figure 2.3-1 Retaining Screen and SS perforated air pipe in MBBR Tank

As the biofilm grows a natural “sloughing” of the bio-film off the bio-carriers occurs. That sloughing maintains the biofilm at a thickness supported by the incoming organic load. Biomass that sloughs off passes through the effluent sieve. Clarification/sedimentation is then employed to remove the sloughed off biomass from the treated leachate. The biofilm carrier elements are made of high density polyethylene and have a specific gravity of 0.96.

The MBBR treatment process can offer numerous advantages over a suspended growth activated sludge treatment process. Those advantages include:  Resilient Treatment Population: The bio-carriers provide the bio-films a protected environment. That protected environment often translates to providing a more resilient treatment population.  Denser treatment population per unit volume: The treatment population per unit volume is denser compared to conventional suspended growth activated sludge systems. That often translates into smaller treatment volumes (i.e. smaller foot print) and greater capacity to successfully treat incoming organic loads.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-14

 Focus on Specific Treatment Populations: Within the biofilm layers develop favouring specific types of treatment organisms. That enables the biofilms to develop specifically focused for the organic load.  Energy efficient  Small foot print: MBBR footprint is smaller than comparable aerated leachate treatment systems for either industrial or municipal leachates.  Easy to operate: MBBR system does have a Return Activated Sludge component or sludge wasting.

High Loading Conditions: The ability of the biofilm to grow as organic loading increases enables a MBBR process to successfully handle extremely high loading conditions with very little operator intervention.

Biofilms are communities of microorganisms growing on surfaces. The microorganisms in the biofilms are essentially the same as those in suspended activated sludge leachate treatment systems. Most of the microorganisms in the biofilm are heterotrophic (they use organic carbon to create new biomass), with facultative bacteria predominating. Facultative bacteria can use the dissolved oxygen in the mixed liquor or, if dissolved oxygen is not available, they will utilize the available nitrate/nitrite as electron acceptors.

Figure 2.3-2 BioChip after 4 weeks of operation

Figure 2.3-3 BioChip after 16 weeks of operation

At the surface of the biofilm is a stagnant liquid layer that separates the biofilm from the moving mixed liquor in the reactor. Nutrients and oxygen diffuse across the stagnant liquid layer from the moving mixed liquor to the biofilm. While nutrients (substrates) and oxygen diffuse through the stagnant layer to the biofilm, biodegradation products diffuse outward from the biofilm to the moving mixed liquor. These “back and forth” diffusion processes are continuous. Figure 6 above shows these diffusion processes.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-15

As the microorganisms grow and multiply, the biomass on the BioMedia grows or thickens. Biomass thickening affects the ability of dissolved oxygen and substrate in the reactor to “reach” all of the biofilm microorganisms. Microorganisms in the outer layers of the biofilm have “first access” to the dissolved oxygen and substrate diffusing through the biofilm. As the dissolved oxygen and substrate diffuses through each subsequent layer in the biofilm, more and more is consumed by the microorganisms in the preceding biofilm layers. The decrease of available dissolved oxygen through the biofilm produces aerobic, anoxic and anaerobic layers in the biofilm.

Different biological action occurs in each of those layers as specific microorganisms grow in the different environments within the biofilm. An examination of the microorganisms in each layer of the biofilm will show a population best suited for the oxygen/substrate environment in that layer. In the upper layers of the biofilm, where dissolved oxygen and substrate concentrations are high, the microorganism population will be aerobic higher level organisms. Deeper into the biofilm, where the oxygen and substrate concentrations decrease, facultative bacteria are the predominant microorganism present. In those layers nitrification occurs as nitrates become “electron acceptors of choice” for the facultative bacteria.

Eventually, microorganisms at the biofilm/bio-carrier interface will be adversely affected by the decrease in substrate and oxygen reaching their layer in the biofilm. As the microorganisms in the biofilm’s attachment layer weaken, the shearing action of the moving mixed liquor washes the biofilm away from the BioMedia. The washing away process, referred to as sloughing, is a function of both hydraulic and loading rates in the reactor.

2.3.4. Aerobic Biological Treatment: Activated Sludge Process (ASP)

a) Activated sludge is a colony of mixed aerobic microbes, namely bacteria, protozoa, mold, yeast, algae, etc. The activated sludge method is a water purification process using the life activity of the activated sludge. In other words, the activated sludge added into leachate absorbs and takes in organic matters contained in the leachate. In this way, organic matters are removed out of system in the way of assimilation or dissimilation.

Organic matters + Activated Adsorption Organic matter = Activated Enzyme Sludge Sludge

Enzyme action Intake of organic matter Growth of activated + Water + Carbon sludge dioxide

Oxygen + Nutrient + Powdered Activated Carbon

b) As apparent from the above, it is very important to acclimate bacteria which provides suitable enzyme to decompose organic matters in leachate. Enzyme function is controlled by water temperature, pH, organic matter concentration, heavy metal ions. Well balanced nutrient is important for the microbes to grow in leachate. Nutrient shall be dosed in to enhance the growth of suitable bacteria.

c) Microorganisms use the organic in leachate as a food supply and convert them into biological cells or biomass. Since leachate contains a wide variety of organic matters a wide variety of organisms or a mixed culture utilities the food source most suitable for its metabolism.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-16

d) Powdered activated carbon shall be added to enhance the treatment efficiency especially the removal of slowly and non-biodegradable COD. Air is supplied into the aeration tanks using blower via diffusers. Surface Aerator c/w Mixer will be installed to enable the effluent in the ASP Tank remained aerated and mixed.

Figure 2.3-4 Air distribution pipe from air blower to air diffusers inside the ASP Tank

Figure 2.3-5 Surface aerator in the ASP to ensure there is enough oxygen for biological degradation

2.3.5. Biological Clarifier

a) After ASP Tank, the water overflows into Degassing Tank prior flow to Biological Clarifier before further Physical-Chemical Treatment. b) Biological Clarifier functions as an efficient solid liquid separator. The settled mixed liquor suspended solids (MLSS) is recycled back to MBBR Tank 1 and ASP Tank as return activated sludge (RAS). The excess MLSS is transferred to Sludge Holding Tank as waste activated sludge (WAS). c) The supernatant shall flow to Mixing Tank 1 / 2 for further physical-chemical treatment.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-17

Figure 2.3-6 Biological Clarifier with Mechanical Scrapping System

2.3.6. Physical-Chemical Treatment

a) The chemical treatment is consist of Mixing Tank, Flocculation Tank and Inclined Plate Clarifier.

b) Coagulant, pH Adjuster and Polymer will be dosed in automatically by dosing pumps into the Mixing Tank & Flocculation Tank.

Note: Type and dosage of chemical to be determined / confirmed based on Jar Test.

c) After chemical treatment, the effluent will gravity flow to Inclined Plate Clarifier (IPC) for further Physical Treatment.

d) IPC is designed to remove particulates from liquids. It consists of a series of closely spaced flat plates inclined at an angle of from 45 to 60 degrees from horizontal. These inclined plates provide a large effective settling area for a small footprint. The inlet stream is stilled upon entry into the clarifier. Solid particles begin to settle on the plates and begin to accumulate in collection hoppers at the bottom of the clarifier unit. The sludge is drawn off at the bottom of these hoppers and the clarified liquid exits the unit at the top by weir.

Figure 2.3-7 Inclined Plate Clarifier ______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-18

2.3.7. Filtration System

a) Treated water from IPC overflows into Clarified Water Tank for storage before pumping to Sand Filter.

b) This water is further treated to remove suspended solids in the passage of water flowing through a bed of sand contained in the Sand Filter. The filtered water is stored in Filtered Water Tank before being used to clean the belt cloths of the Belt Press.

c) Excess water in the Treated Water Tank overflows to Treated Water Pond and Public Drain as Final Discharge.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-19

2.3.8. Sludge Management

a) Sludge management is designed based on the capacity of the leachate treatment plant.

b) The sludge that stored in the Sludge Holding Tank, is transferred to Belt Press for dewatering. The submersible mixer will be used to ensure well mixing of the sludge in the Sludge Holding Tank. Polymer will be dosed automatically by a pump at the inlet of the Belt Press.

c) The filtrate from dewatering process will flow to a Filtrate Sump before recycled back into the Collection Pond. The sludge cake generated from the Belt Press is dry enough and easily to handle. The sludge cake is managed as per local authority guidelines.

Figure 2.3-8 Auto Polymer Preparation

Figure 2.3-9 Belt Press with polymer conditioning tank, drum thickener and squeezing rolls for drier sludge cake

Figure 2.3-10 Sludge cake generated from the Belt Press

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-20

2.4. DESIGN CALCULATION

Note:  Calculation is based on the maximum value of the non-compliance parameters as stated in Section 2.2.  Assumed removal of the stated non-compliance parameter from the leachate.  The following calculation (biological-physical-chemical) have been based on three (3) technical references: a. W. Wesley Eckenfelder, Jr., Industrial Water Pollution Control, Third Edition; pg 112, pg 128, pg 129. b. Metcalf & Eddy, Wastewater Engineering, Fourth Edition; pg 687, 1002. c. Metcalf & Eddy, Wastewater Engineering, Third Edition; pg 247, 303, 488, 473, 548, 550  The treatability information and literature records of the proposed coagulant and oxidizer and decolorization agent, i.e. Ferrate VI, a green chemical for wastewater treatment has been included in Section 2.4.10

Equipment and Tanks Sizing / Sizing Calculation

2.4.1. Collection Pond

Quantity : One (1) unit Capacity : 15,000 m3 Flowrate : 83.33 m3/hr Retention Time : 15,000 m3 / 83.33 m3/hr = 7.5 day

2.4.2. Anaerobic MBBR Tank 1 / 2

Quantity : Two (2) units Capacity : 380 m3 each tank Dimension : ⌀ 7.8 m x 8 m(H) Flowrate : 83.33 m3/hr Retention Time : (380 x 2) m3 / 83.33 m3/hr = 9.12 hours

COD Loading : [(15,000 - 2,250) mg/L x 2,000 m3/day] / 1,000 : 25,500 kg/m3.day

Use biochip COD Load: 100 kg/m3.day

Biochip Volume : 192 m3 (biochip with surface area: 4,000 m2/m3)

For Mass Balance Calculation (Anaerobic MBBR Tanks)

Removal Efficiency : 85% in BOD 85% in COD

Treated Effluent BOD : 15% x 10,000 ppm = 1,500 ppm Removal BOD : 85% x 10,000 ppm = 8,500 ppm

Treated Effluent COD : 15% x 15,000 ppm = 2,250 ppm Removal COD : 85% x 15,000 ppm = 12,750 ppm

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-21

2.4.3. Primary Clarifier

Quantity : One (1) unit Effective Capacity : 530 m3 Dimension : ⌀ 12 m x 4.5m(H) Flowrate : 83.33 m3/hr Up-flow : 0.7 m/hr Area : 83.33 m3/hr / 0.7 m/hr = 119.05 m2 Scrapper Diameter : 12 m

2.4.4. Buffer Tank

Quantity : One (1) unit Capacity : 40 m3 Dimension : 3.4 m(L) x 3.4 m(W) x 4.5m(H) Flowrate : 83.33 m3/hr Retention Time : 40 m3 / 83.33 m3/hr = 30 mins

2.4.5. Moving Bed Biofilm Reactor (MBBR Tank)

Quantity : Three (3) units Eff. Volume : 500 m3 Dimension : 5.6 m(L) x 11.9 m(W) x [7.5 + 0.5FB] m(H) Flowrate : 83.33 m3/hr Retention Time : 500 m3 / 83.33 m3/hr = 6 hrs

a. MBBR Tank 1

Design Calculation for the MBBR BioChip Volume

Capacity : 2,000 m3/d : 83.33 m3/hr @ 24 hr/day Influent BOD5 : 1,500 mg/L Influent COD : 2,250 mg/L

Given, from COD load vs removal rate Graph: 3 COD Load, x = 80 kg/m c.day COD Removal Rate, y = 9.58 + 0.46102x 3 = 46.46 kg/m c.day

i) COD Loading = 1,800 kg/day BioChip Volume = 1,800 kg/day 3 80 kg/m c.day 3 = 22.5 m c (Removal rate: 58.08%) 3 Proposed Volume = 12 m c (biochip with surface area: 4,000 m2/m3)

ii) Based on Proposed BioChip Volume, 3 3 Actual COD Removal = 46.46 kg/m c.day x 16 m c = 743.39 kg/day Effluent COD = 1,878.31 ppm COD Removal Rate = 41.3 %

Design Calculation for the Tank Volume and Air Requirement

i) Determine total amount of soluble BOD5 for effluent.

By assuming the characteristic of effluent, Suspended solid (SS) = 1,000 mg/L Biodegradable fraction of SS = 0.65 Ratio of BOD5 to BODL = 0.68 Ratio of oxygen to cell = 1.42 g O2/g BOD5 Hence, BOD5 of effluent SS = 627.64 mg/L ______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-22

Effluent BOD5, Se,total = Influent soluble BOD5 escaping treatment, Se,sol + BOD5 of effluent SS , Se,SS

Hence, Influent soluble BOD5 escaping treatment, Se,sol = 272.36 mg/L

ii) Determine the treatment efficiency based on soluble BOD5 and overall plant. Generally, treatment efficiency, E = [(S0 – S) / S0] x 100

Treatment efficiency based on soluble BOD5, ES = 81.84 % (A) The overall plant efficiency, Eoverall = 40 % (B) (Make sure that the value of A is higher than B)

iii) MBBR Tank Volume

Retention time, RT = 2 hr Tank Volume = 166.67 m3 Tank Height = 7.5 m + 0.5 m FB Tank surface area = 22.22 m2

iv) Determine the oxygen demand to the aeration process.

Oxygen demand = Total mass of BODL utilized (AOTR) = 1.47 Q (S0-Se,sol) = 150.39 kg/h

v) Design Data (Air Supply):

Oxygen demand (AOTR) = 150.39 kg/h Height of tank = 7.5 m Tank surface area (aerated) = 22.22 m2 Tank volume = 166.67 m3 Temperature of wastewater = 40 °C Altitude of treatment plant = 20 m above sea level (assumed)

Values given:

Immersion depth of pipe aerator, D = 7.8 m Beta, β = 0.98 Alpha, a = 0.6 Theta, q = 1.024 Specific airflow = 7.5 Nm3/h.m 3 Specific oxygen absorption, SOA = 9 g O2/Nm .m Operating dissolved O2 conc, CL = 3 mg/L Dissolved O2 conc. at 20°C, CS,20 = 9.08 mg/L Dissolved O2 conc. at 25°C = 8.24 mg/L

Calculation:

a) Determine the relative pressure to get the DO value with respect to the altitude of the treatment plant.

Given that altitude of the treatment plant is 20m above the sea level, From Appendix B (Metcalf & Eddy, 4th Ed.),

Where, g = 9.81 m/s2 M = 28.97 kg/kmole R = 8,314 kgm2/s2.kmol.K T = 313.15 K @ 40°C

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-23

Relative pressure at elevation 20 m = 0.998

Concentration of O2 at 25°C & 20m, CS,TH = Relative pressure at elevation 20m x Dissolved O2 conc. at 25°C = 8.222 mg/L

b) Determine the atmospheric pressure of water at 20m, 25°C in metres of water, Patm,H

Given that atm. Pressure of water at given altitude and temperature = Relative pressure at elevation 20m x Psea level Specific weight of water Where Psea level = 101.325 kPa At T = 40°C Specific weight of water = 9.7265 kN/m3

Atm. Pressure of water at 20m, 40°C, Patm,H = 10.395 m WC

c) Determine the amount of O2 transfer to and leaving from water to obtain the average dissolved oxygen (DO) saturation concentration.

Molecular mass of O2 = 6.704 kg O2 Molecular mass of air = 28.97 kg air Ratio of O2 to air = 0.231 kg O2 / kg air Air density at 20m above sea level = 1.29 kg air / m3 air

Fraction of O2 transferred to water = SOA x immersion depth of pipe aerator Ratio of O2 to air x Air density = 0.235

Percentage of O2 in air leaving water, Ot = Oxygen leaving water x 100% Air leaving water Composition of air, O2 = 21% N2 = 79%

% of O2 in air leaving water, Ot = 21 x (1-Fraction) x 10 79 + 21 (1-Fraction) = 0.169 = 16.9 %

Average dissolved oxygen saturation concentration, Cave S, TH

=

= 7.19 mg/L

d) Determine Standard Oxygen Transfer Rate (SOTR)

SOTR = 350 kg/h

e) Determine the required airflow, aeration length and surface.

Required airflow = SOTR Aeration depth x SOA = 4,986 Nm3/h = 83.095 Nm3/min [A]

Air mixing = 15 m3/m2/hr x (500/5)m2 = 1,500 m3/hr = 25 m3/min [B]

Since [A] is greater, thus the required airflow to be used is 83.1 m3/min

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-24

For Mass Balance Calculation (MBBR Tank 1)

Removal Efficiency : 40% in BOD : 40% in COD : 60% in Ammoniacal Nitrogen (A-N)

Treated Effluent BOD : 60% x 1,500 ppm = 900 ppm Removal BOD : 40% x 1,500 ppm = 600 ppm

Treated Effluent COD : 60% x 2,250 ppm = 1,350 ppm Removal COD : 40% x 2,250 ppm = 900 ppm

Treated Effluent A-N : 40% x 1,500 ppm = 600 ppm Removal A-N : 60% x 1,500 ppm = 900 ppm

b. MBBR Tank 2

Design Calculation for the MBBR BioChip Volume

Capacity : 2,000 m3/d : 83.33 m3/hr @ 24 hr/day Influent BOD5 : 900 mg/L Influent COD : 1,350 mg/L

Given, from COD load vs removal rate Graph: 3 COD Load, x = 50 kg/m c.day COD Removal Rate, y = 9.58 + 0.46102x 3 = 32.63 kg/m c.day

i) COD Loading = 1,080 kg/day BioChip Volume = 1,080 kg/day 3 50 kg/m c.day 3 = 21.6 m c (Removal rate: 65.26%) Proposed Volume = 10.5 m3 (biochip with surface area: 4,000 m2/m3)

ii) Based on Proposed BioChip Volume, 3 3 Actual COD Removal = 32.63 kg/m c.day x 14 m c = 456.83 kg/day Effluent COD = 1,121.58 ppm COD Removal Rate = 42.3 %

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-25

Design Calculation for the Tank Volume and Air Requirement

i) Determine total amount of soluble BOD5 for effluent.

By assuming the characteristic of effluent, Suspended solid (SS) = 800 mg/L Biodegradable fraction of SS = 0.65 Ratio of BOD5 to BODL = 0.68 Ratio of oxygen to cell = 1.42 g O2/g BOD5 Hence, BOD5 of effluent SS = 502.11 mg/L Effluent BOD5, Se,total = Influent soluble BOD5 escaping treatment, Se,sol + BOD5 of effluent SS , Se,SS

Hence, Influent soluble BOD5 escaping treatment, Se,sol = 37.89 mg/L

ii) Determine the treatment efficiency based on soluble BOD5 and overall plant. Generally, treatment efficiency, E = [(S0 – S) / S0] x 100 Treatment efficiency based on soluble BOD5, ES = 95.79 % (A) The overall plant efficiency, Eoverall = 40 % (B) (Make sure that the value of A is higher than B)

iii) MBBR Tank Volume

Retention time, RT = 2 hr Tank Volume = 166.67 m3 Tank Height = 7.5 m + 0.5 m FB Tank surface area = 22.22 m2

iv) Determine the oxygen demand to the aeration process. Oxygen demand = Total mass of BODL utilized (AOTR) = 1.47 Q (S0-Se,sol) = 105.61 kg/h

v) Design Data (Air Supply):

Oxygen demand (AOTR) = 105.61 kg/h Height of tank = 7.5 m Tank surface area (aerated) = 22.22 m2 Tank volume = 166.67 m3 Temperature of wastewater = 40 °C Altitude of treatment plant = 20 m above sea level (assumed)

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-26

Values given:

Immersion depth of pipe aerator, D = 7.8 m Beta, β = 0.98 Alpha, a = 0.6 Theta, q = 1.024 Specific airflow = 7.5 Nm3/h.m 3 Specific oxygen absorption, SOA = 9 g O2/Nm .m Operating dissolved O2 conc, CL = 3 mg/L Dissolved O2 conc. at 20°C, CS,20 = 9.08 mg/L Dissolved O2 conc. at 25°C = 8.24 mg/L

Calculation:

a) Determine the relative pressure to get the DO value with respect to the altitude of the treatment plant.

Given that altitude of the treatment plant is 20m above the sea level, From Appendix B (Metcalf & Eddy, 4th Ed.),

Where, g = 9.81 m/s2 M = 28.97 kg/kmole R = 8,314 kgm2/s2.kmol.K T = 313.15 K @ 40°C

Relative pressure at elevation 20 m = 0.998

Concentration of O2 at 25°C & 20m, CS,TH = Relative pressure at elevation 20m x Dissolved O2 conc. at 25°C = 8.222 mg/L

b) Determine the atmospheric pressure of water at 20m, 25°C in metres of water, Patm,H

Given that atm. Pressure of water at given altitude and temperature = Relative pressure at elevation 20m x Psea level Specific weight of water Where Psea level = 101.325 kPa At T = 40°C Specific weight of water = 9.7265 kN/m3

Atm. Pressure of water at 20m, 40°C, Patm,H = 10.395 m WC

c) Determine the amount of O2 transfer to and leaving from water to obtain the average dissolved oxygen (DO) saturation concentration.

Molecular mass of O2 = 6.704 kg O2 Molecular mass of air = 28.97 kg air Ratio of O2 to air = 0.231 kg O2 / kg air Air density at 20m above sea level = 1.29 kg air / m3 air

Fraction of O2 transferred to water = SOA x immersion depth of pipe aerator Ratio of O2 to air x Air density = 0.235

Percentage of O2 in air leaving water, Ot = Oxygen leaving water x 100% Air leaving water Composition of air, O2 = 21% N2 = 79%

% of O2 in air leaving water, Ot = 21 x (1-Fraction) x 10 79 + 21 (1-Fraction) = 0.169

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-27

= 16.9 %

Average dissolved oxygen saturation concentration, Cave S, TH

=

= 7.19 mg/L

d) Determine Standard Oxygen Transfer Rate (SOTR)

SOTR = 245.79 kg/h

e) Determine the required airflow, aeration length and surface.

Required airflow = SOTR Aeration depth x SOA = 3,501.23 Nm3/h = 58.35 Nm3/min [A]

Air mixing = 15 m3/m2/hr x (500/5)m2 = 1,500 m3/hr = 25 m3/min [B]

Since [A] is greater, thus the required airflow to be used is 58.35 m3/min

For Mass Balance Calculation (MBBR Tank 2)

Removal Efficiency : 40% in BOD : 40% in COD : 60% in Ammoniacal Nitrogen (A-N)

Treated Effluent BOD : 60% x 900 ppm = 540 ppm Removal BOD : 40% x 900 ppm = 360 ppm

Treated Effluent COD : 60% x 1,350 ppm = 810 ppm Removal COD : 40% x 1,350 ppm = 540 ppm

Treated Effluent A-N : 40% x 600 ppm = 240 ppm Removal A-N : 60% x 600 ppm = 360 ppm

c. MBBR Tank 3

Design Calculation for the MBBR BioChip Volume

Capacity : 2,000 m3/d : 83.33 m3/hr @ 24 hr/day Influent BOD5 : 540 mg/L Influent COD : 810 mg/L

Given, from COD load vs removal rate Graph: 3 COD Load, x = 30 kg/m c.day COD Removal Rate, y = 9.58 + 0.46102x 3 = 23.41 kg/m c.day

i) COD Loading = 486 kg/day BioChip Volume = 486 kg/day 3 30 kg/m c.day 3 = 16.2 m c (Removal rate: 78.04%) 3 Proposed Volume = 6 m c (biochip with surface area: 4,000 m2/m3)

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-28

ii) Based on Proposed BioChip Volume, 3 3 Actual COD Removal = 23.41 kg/m c.day x 8 m c = 187.28 kg/day Effluent COD = 716.36 ppm COD Removal Rate = 38.54 %

Design Calculation for the Tank Volume and Air Requirement

i) Determine total amount of soluble BOD5 for effluent.

By assuming the characteristic of effluent, Suspended solid (SS) = 600 mg/L Biodegradable fraction of SS = 0.65 Ratio of BOD5 to BODL = 0.68 Ratio of oxygen to cell = 1.42 g O2/g BOD5 Hence, BOD5 of effluent SS = 376.58 mg/L Effluent BOD5, Se,total = Influent soluble BOD5 escaping treatment, Se,sol + BOD5 of effluent SS , Se,SS

Hence, Influent soluble BOD5 escaping treatment, Se,sol = 1.416 mg/L

ii) Determine the treatment efficiency based on soluble BOD5 and overall plant. Generally, treatment efficiency, E = [(S0 – S) / S0] x 100 Treatment efficiency based on soluble BOD5, ES = 99.74 % (A) The overall plant efficiency, Eoverall = 30 % (B) (Make sure that the value of A is higher than B)

iii) MBBR Tank Volume

Retention time, RT = 2 hr Tank Volume = 166.67 m3 Tank Height = 7.5 m + 0.5 m FB Tank surface area = 22.22 m2

iv) Determine the oxygen demand to the aeration process. Oxygen demand = Total mass of BODL utilized (AOTR) = 1.47 Q (S0-Se,sol) = 65.98 kg/h

v) Design Data (Air Supply):

Oxygen demand (AOTR) = 65.98 kg/h Height of tank = 7.5 m Tank surface area (aerated) = 22.22 m2 Tank volume = 166.67 m3 Temperature of wastewater = 40 °C Altitude of treatment plant = 20 m above sea level (assumed)

Values given:

Immersion depth of pipe aerator, D = 7.8 m Beta, β = 0.98 Alpha, a = 0.6 Theta, q = 1.024 Specific airflow = 7.5 Nm3/h.m 3 Specific oxygen absorption, SOA = 9 g O2/Nm .m Operating dissolved O2 conc, CL = 3 mg/L Dissolved O2 conc. at 20°C, CS,20 = 9.08 mg/L Dissolved O2 conc. at 25°C = 8.24 mg/L

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-29

Calculation:

a) Determine the relative pressure to get the DO value with respect to the altitude of the treatment plant.

Given that altitude of the treatment plant is 20m above the sea level, From Appendix B (Metcalf & Eddy, 4th Ed.),

Where, g = 9.81 m/s2 M = 28.97 kg/kmole R = 8,314 kgm2/s2.kmol.K T = 313.15 K @ 40°C Relative pressure at elevation 20 m = 0.998

Concentration of O2 at 25°C & 20m, CS,TH = Relative pressure at elevation 20m x Dissolved O2 conc. at 25°C = 8.222 mg/L

b) Determine the atmospheric pressure of water at 20m, 25°C in metres of water, Patm,H

Given that atm. Pressure of water at given altitude and temperature = Relative pressure at elevation 20m x Psea level Specific weight of water Where Psea level = 101.325 kPa At T = 40°C Specific weight of water = 9.7265 kN/m3

Atm. Pressure of water at 20m, 40°C, Patm,H = 10.395 m WC

c) Determine the amount of O2 transfer to and leaving from water to obtain the average dissolved oxygen (DO) saturation concentration.

Molecular mass of O2 = 6.704 kg O2 Molecular mass of air = 28.97 kg air Ratio of O2 to air = 0.231 kg O2 / kg air Air density at 20m above sea level = 1.29 kg air / m3 air

Fraction of O2 transferred to water = SOA x immersion depth of pipe aerator Ratio of O2 to air x Air density = 0.235 Percentage of O2 in air leaving water, Ot = Oxygen leaving water x 100% Air leaving water Composition of air, O2 = 21% N2 = 79%

% of O2 in air leaving water, Ot = 21 x (1-Fraction) x 10 79 + 21 (1-Fraction) = 0.169 = 16.9 %

Average dissolved oxygen saturation concentration, Cave S, TH

=

= 7.19 mg/L

d) Determine Standard Oxygen Transfer Rate (SOTR)

SOTR = 153.55 kg/h

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-30

e) Determine the required airflow, aeration length and surface.

Required airflow = SOTR Aeration depth x SOA = 2,187.32 Nm3/h = 36.46 Nm3/min [A]

Air mixing = 15 m3/m2/hr x (500/5)m2 = 1,500 m3/hr = 25 m3/min [B]

Since [A] is greater, thus the required airflow to be used is 36.46 m3/min

For Mass Balance Calculation (MBBR Tank 3)

Removal Efficiency : 30% in BOD : 30% in COD : 60% in Ammoniacal Nitrogen (A-N)

Treated Effluent BOD : 70% x 540 ppm = 378 ppm Removal BOD : 30% x 540 ppm = 162 ppm

Treated Effluent COD : 70% x 810 ppm = 567 ppm Removal COD : 30% x 810 ppm = 243 ppm

Treated Effluent A-N : 40% x 240 ppm = 96 ppm Removal A-N : 60% x 240 ppm = 144 ppm

2.4.6. Activated Sludge Process (ASP)

Quantity : One (1) units Capacity : 2,500 m3 Dimension : 17.4 m(L) x 19.7 m(W) x [7.3 + 0.7FB] m(H) Flowrate : 83.33 m3/hr Retention Time : 2,500 m3 / 83.33 m3/hr = 30 hrs (1.25 days)

Design Data: Influent Flowrate, Q = 2,000 m3/d Influent BOD5, S0 = 378 mg/L Effluent BOD5, Se,total = 76 mg/L Aeration tank Temperature = 40 °C Yield Coefficient, Y = 0.6 gVSS/gBOD5 -1 Decay Constant, Kd = 0.06 d Mean Cell Residence Time, θc = 30 day Mixed-liquor Volatile Suspended Solid (MLVSS), Xvss = 3,200 mg/L Mixed-liquor Suspended Solid (MLSS), XTSS = 4,000 mg/L Ratio of MLVSS : MLSS = 0.8 Recycle Sludge of Suspended Solid = 11,000 mg/L Recycle Sludge (MLVSS), Xr = 8,800 mg/L

Calculation:

a) Determine total amount of soluble BOD5 for effluent,

By assuming the characteristic of effluent, Suspended Solid (SS) = 100 mg/L Biodegradable Fraction of SS = 0.65 (65% is biodegradable) Ration of BOD5 to BODL = 0.68 Ration of Oxygen to Cell = 1.42 g O2 / g BOD5 Hence, BOD5 of effluent SS = 62.764 mg/L Effluent BOD5, Se,total = Influent soluble BOD5, escaping treatment, Se,total + BOD5 of effluent SS, Se,SS Hence, Influent soluble BOD5 escaping treatment, Se,sol = 12.836 mg/L

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-31

b) Determine the treatment efficiency based on soluble BOD5, and overall plant.

Generally, treatment efficiency, E = [(S0 – S) / S0] x 100

Treatment Efficiency based on soluble BOD5, Es = 96.6 % (A) The overall plant efficiency, Eoverall = 80 % (B)

To make sure value (A) is higher than (B)

c) Determine the volume of tank, V and hydraulic retention time, θ.

where, Y = 0.6 g VSS / g BOD5 Q = 2,000 m3/d θc = 30 d S0 = 378 mg/L Se,sol = 12.84 mg/L -1 Kd = 0.06 d XVSS = 3,200 mg/L

Calculated aeration tank volume, V = 1,467 m3 Proposed aeration tank volume, V = 2,500 m3 Hydraulic Retention = Aeration tank volume Time, θ Influent flowrate = 30 hour = 1.25 day

d) Determine the amount of waste sludge produced each day. To determine the observed yield,

where, Y = 0.6 g VSS / g BOD5 θc = 30 d -1 Kd = 0.06d

Observed yield, Yobs = 0.2143 To determine the increase in mass of MLVSS in reactor, PX(VSS) = YobsQ(S0-Se,sol) where, Yobs = 0.2143 Q = 2,000 m3/d S0 = 378 mg/L Se,sol = 12.84 mg/L

Mass of MLVSS increase in reactor, PX(VSS) = 156.5 kg/d

The increase in total mass of MLSS in reactor, PX(SS) = 195.624 kg/d

Mass to be wasted = Increase in MLSS – SS lost in effluent = 4.38 kg/d [A] From recycle line, calculate the mass of sludge (MLVSS) wasting per day.

By using

Where, V = 2,500 m3 X = 3,200 mg/L θc = 30 d Xr = 8,800 mg/L 3 Sludge wasting, Q’W = 37.88 m /d = 1.578 m3/h To calculate mass of sludge wasting, Q’W x Xr = 266.67 kg/d [B]

By comparing [A] and [B], choose the higher one. Hence, mass of the sludge need to be wasted = 266.67 kg/d

e) Determine the recirculation ratio.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-32

Recirculation ratio,

By neglecting the effluent biomass concentration, Xe = 0 R = 0.5 417

f) Determine the oxygen demand to the aeration process. Oxygen demand = Total mass of BODL utilized – 1.42 (Mass of sludge wasted) AOTR = 1.47 Q (S0-Se,sol) – 1.42 (Q’WXr) = 28.95 kg/h

g) Check the F/M ration and the volumetric loading factor.

From , F/M = 0.095 d-1

From

3 Volumetric loading = 0.3024 kg BOD5 / m .d

h) Design Data (Air Supply): Oxygen demand (AOTR) = 28.95 kg/h Height of tank = 7.3 m Tank surface area (aerated) = 342.47 m2 Tank volume = 2,500 m3 Temperature of wastewater = 40°C Altitude of treatment plant = 20 m above sea level (assumed)

Values Given: Immersion depth of pipe aerator, D = 7.8 m Bate, β = 0.98 Alpha, α = 0.6 Theta, θ = 1.024 Specific airflow = 7.5 Nm3/h.m 3 Specific oxygen absorption, SOA = 9 g O2/Nm .m Operating dissolved O2 conc., CL = 4 mg/L Dissolved O2 conc. at 20°C, CS,20 = 9.08 mg/L Dissolved O2 conc. at 11°C = 11.02 mg/L

Calculation:

1) Determine the relative pressure to get the DO value with respect to the altitude of the treatment plant.

Given that altitude of the treatment plant is 20m above the sea level, From Appendix B (Metcalf & Eddy, 4th Ed.),

Where, g = 9.81 m/s2 M = 28.97 kg/kmole R = 8,314 kgm2/s2.kmol.K T = 313.15 K @ 40°C

Relative pressure at elevation 20 m = 0.9978

Concentration of O2 at 11°C & 20m, CS,TH = Relative pressure at elevation 20m x Dissolved O2 conc. at 11°C = 10.996 mg/L

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-33

2) Determine the atmospheric pressure of water at 20m, 11°C in metres of water, Patm,H Given that atm. Pressure of water at given altitude and temperature = Relative pressure at elevation 20m x Psea level Specific weight of water

Where Psea level = 101.325 kPa *Specific weight of water at 11°C

At T = 40°C Specific weight of water = 9.7265 kN/m3

Atm. Pressure of water at 20m, 11°C, Patm,H = 10.3947 m WC

3) Determine the amount of O2 transfer to and leaving from water to obtain the average dissolved oxygen (DO) saturation concentration. Molecular mass of O2 = 6.704 kg O2 Molecular mass of air = 28.97 kg air Ratio of O2 to air = 0.231 kg O2 / kg air Air density at 20m above sea level = 1.29 kg air / m3 air

Fraction of O2 transferred to water = SOA x immersion depth of pipe aerator Ratio of O2 to air x Air density = 0.235

Percentage of O2 in air leaving water, Ot = Oxygen leaving water x 100% Air leaving water Composition of air, O2 = 21% N2 = 79% % of O2 in air leaving water, Ot = 21 x (1-Fraction) x 10 79 + 21 (1-Fraction) = 0.169 = 16.9%

Average dissolved oxygen saturation concentration, Cave S, TH

=

= 9.616 mg/L

4) Determine Standard Oxygen Transfer Rate (SOTR)

SOTR = 50.28 kg/h

5) Determine the required airflow, aeration length and surface.

Required airflow = SOTR Aeration depth x SOA = 716.17 Nm3/h = 11.94 Nm3/min [A]

Air mixing = 0.01m3/m3/min x 2,500 m3 = 25 m3/min [B]

Since Air mixing is greater, thus the required airflow to be used is 25 m3/min

For Mass Balance Calculation (ASP Tank)

Removal Efficiency : 80% in BOD 70% in COD 95% in Ammoniacal Nitrogen (A-N)

Treated Effluent BOD : 20% x 378 ppm = 75.6 ppm

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-34

Removal BOD : 80% x 378 ppm = 302.4 ppm

Treated Effluent COD : 30% x 567 ppm = 170.1 ppm Removal COD : 70% x 567 ppm = 396.9 ppm

Treated Effluent A-N : 5% x 96 ppm = 4.8 ppm Removal A-N : 95% x 96 ppm = 91.2 ppm

2.4.7. Degassing Tank

Quantity : One (1) unit Capacity : 30 m3 Dimension : 1.5 m(L) x 2.9 m(W) x [7.1 + 0.4FB] m(H) Flowrate : 2 x 83.33 m3/hr = 166.67 m3/hr Retention Time : 30 m3 / 166.67 m3/hr = 10 mins

2.4.8. Biological Clarifier

Quantity : One (1) unit Effective Capacity : 530 m3 Dimension : ⌀ 12 m x 4.5m(H) Flowrate : 83.33 m3/hr Up-flow : 0.7 m/hr Area : 83.33 m3/hr / 0.7 m/hr = 119.05 m2 Scrapper Diameter : 12 m

Design Data:

Influent Flowrate = 83.33 m3/hr Mixed-liquor Volatile Suspended Solid (MLVSS), Xvss = 3,200 mg/L Mixed-liquor Suspended Solid (MLSS), XTSS = 4,000 mg/L Ratio of MLVSS : MLSS = 0.8 Recycle Sludge (MLVSS), Xr = 8,800 mg/L

Hydraulic Retention Time = 530 m3 / 83.33 m3/hr = 6.36 hours

Effective overflow area = Area of Clarifier = π x 122 / 4 = 113 m2

Overflow rate = Flowrate / Effective overflow area = 83.33 m3/hr / 113 m2 = 0.737 m/hr

(Design parameter: avg 0.33 – 1 m/hr, Metcalf & eddy, 4th Ed., table 8-7) (Q  Q )(X ) Sludge Loading Rate, SLR  R A Where Q = 2,000 m3/day 3 Assume Xr = 8,800 g/m 3 XTSS = 4,000 g/m R = XTss . Xr - XTss = 0.833

Hence, QR = Q x R = 2,000 m3/day x 0.833 = 1,666.67 m3/day

XVSS = 3,200 mg/l; MLSS = MLVSS / 0.8 A = 113 m2

Hence SLR = 103.84 kg/m2 day = 4.326 kg/m2 hr ______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-35

(Design parameter: avg 1.0 - 5.0 kg/m2.h, Metcalf & Eddy, 4th Ed., Table 8-7)

2.4.9. Clarified Water Sump

Quantity : One (1) unit Capacity : 20 m3 Dimension : 3.3 m(L) x 3 m(W) x 2.5 m(Dp) Flowrate : 83.33 m3/hr Retention Time : 20 m3 / 83.33 m3/hr = 15 mins

2.4.10. Mixing Tank 1 / 2 (for RED + OXY Mixing to generate Ferrate VI)

Quantity : Two (2) units Capacity : 7 m3 Dimension : 3 m(L) x 3 m(W) x [3.2 + 0.2FB] m(H) Flowrate : 83.33 m3/hr Retention Time : 20 m3 / 83.33 m3/hr = 15 mins

The chemical treatment shall target to treat a mixture of pollutants at various concentrations (composition) as listed below (extracted from Section 2.2.1), as follows:-

PARAMETER Peak Load Treated Effluent B.O.D, mg/l (5days @ ≤ 10,000 ≤ 20 20 oC) C.O.D, mg/l ≤ 15,000 ≤ 400 Suspended solid, mg/l ≤ 1,000 ≤ 50 Ammonical Nitrogen, ≤ 1,500.0 ≤ 5.0 mg/L Oil & Grease, mg/L ≤ 50.0 ≤ 5.0 Copper, mg/L ≤ 0.5 ≤ 0.2 Manganese, mg/L ≤ 5.0 ≤ 0.2 Boron, mg/L ≤ 10.0 ≤ 1.0 Iron, mg/L ≤ 100.0 ≤ 5.0 Phenol, mg/L ≤ 1.0 ≤ 0.001 Sulphide, mg/L ≤ 5.0 ≤ 0.5 Fluoride, mg/L ≤ 10.0 ≤ 2.0 Formaldehyde, mg/L ≤ 5.0 ≤ 1.0 Colour, ADMI pH (as ≤ 3,000.0 ≤ 100.0 is) Colour, ADMI pH (7.0) ≤ 3,000.0 ≤ 100.0

After the pre-treatment (oil & grease trap), biological treatment (Anaerobic MBBR, MBBR, ASP, Degassing) and physical treated (post-anaerobic clarification and post-anoxic clarification), basically BOD, COD, TSS, A-N and O&G have been removed to comply within the Schedule II discharge standards. However, there remain 10 parameters, including Colour (ADMI) at as is pH and neutral pH, required to be treated.

A green chemical, Ferrate VI has been chosen to be used as coagulant, oxidizer and decolorization agent to carry out the functions to remove these 10 parameters from the effluent.

Appendix 2.2 has included various scientific publications of research findings, including many research references of application and treatability of Ferrate VI in performing the chemical reactions as coagulant, oxidizer and decolorization agent in water and/or wastewater treatment. ______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-36

After a comprehensive review analysis from the relevant scientific publications, the respective stoichiometric equations of Ferrate VI when reacting with the targeted pollutants have been presented in Table 2.4.1.

From the table, it may be noted Ferrate VI has good oxidation reduction potential (ORP) over all the targeted pollutants as above mentioned, at +250-300 mV, and the reaction time requires to achieve reduction (removal) percentage as tabulated is between 10-15 minutesss.

Further to the targeted parameters of heavy metals (copper, manganese, iron), organic (phenol, formaldehyde), inorganic (sulfide, sulfide) and colour, Ferrate VI has the potential to remove between 20-32% of COD and ammoniacal nitrogen (A-N). However, these removal abilities have not been included in the calculation section, and serve as safety buffer for COD and A-N treatment, as these are the two key parameters for final discharge of treated leachate effluent. COD and A-N removal has been targeted to be taken care of during biological-physical treatment processes.

Appendix 2.3 has included a selected Ferrate VI green chemical supplier technical information, whereas has vast experience in supplying and applying Ferrate VI for treatment of various contaminants or pollutants

For the record, a lab-scale OXY-RED Ferrate VI prototype kit shall be assembled to test the treatability of the leachate for the targeted pollutants. This test shall be carried out as part of the design development process to determine the adequate operational dosage for Ferrate VI.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-37

Table 2.4.1 Oxidation Reduction System by Ferrate VI Treatment For Removal of Heavy Metals, Organic, Inorganic Contaminants & Colour

No. Pollutants Influent Load Effluent Percentage Stoichiometric equation of Ferrate (FeVI) pH ORP Reaction (ppm) after Load after Reduction with Pollutants Set Point Set Time Biological Ferrate VI ( % ) (Value) Point (Minute) Treatment Treatment (+mV) 1 COD 400 272 < 32 Total COD Reduction including dissolved and 9.0 250-300 10-15 undissolved COD min

2 Copper 0.5 < 0.1 ( ND ) 90 HFeO4- + Cu(CN)43- + 8H2O → 5Fe(OH)3 + 9.0 250-300 10-15 min 4NCO- + Cu2+ + 6OH- + 3/2 O2 3 Manganese 5 < 0.1 ( ND ) 98 2Fe(VI) + 3Mn(II) → 2Fe(III) + 3Mn(IV) 6.2-7.5 250-300 10-15 min

4 Iron 50 < 5 97 HFeO4- + 3Fe(CN)62- + 3H2O → Fe(OH)3 + 9.0 250-300 10-15 3Fe(CN)63- + min 4OH-

5 Phenol 1 < 0.04 60-70 C6H5OH + 28/3 FeO42- + 61/3H2O → 9.0 250 - 300 10 - 15 min 6 CO2 + 28/3 Fe(OH)3 + 56/3OH 6 Sulfide 5 < 0.3 ( ND ) 98 2HFeO4- + 3SO32- + 3H2O → 2Fe(OH)3 + 9.0 250-300 10-15 min 3SO42- + 2OH-

7 Floride 10 < 2 95 2HeFeO4- + 3F- + OH- → 2Fe(OH)3 + 3FCO- 9.0 250-300 10-15 min

8 Formaldehyde 5 < 1 95 FeO42- + eaq- → FeO43- 9.0 250 - 300 10 - 15 min FeO42- + RĊOH → HFeO42- + RCO 9 Ammonical 5 4 20 2K2Fe04 + 2NH3 + (n-1) H20—»N2 + 8.5 250-300 10-15 Nitrogen Fe2O3.nH2O + 4KOH min 10 Color ( ADMI ) 1000 < 100 92 Removal efficiency to be confirmed by RED-OXY 9.0 250-300 10-15 Lab min

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-38

2.4.11. Flocculation Tank (for ABSORB Mixing)

Quantity : One (1) unit Capacity : 20 m3 Dimension : 6 m(L) x 3 m(W) x [3.2 + 0.2FB] m(H) Flowrate : 83.33 m3/hr Retention Time : 20 m3 / 83.33 m3/hr = 15 mins

2.4.12. Inclined Plate Clarifier (IPC)

Quantity : One (1) unit Flowrate : 2,000 m3/day Design Flowrate : 83.33 m3/hr Dimension : 4.1 m(L) x 2.9 m(W) x 6.43 m(H) No. of Plate : 80 pcs. Single Plate Size : 2,440 mm x 1,260 mm Inclined Angle, θ : 55˚ Effective Capacity : 119 m3 Retention Time : 119 m3 / 83.33 m3/hr = 1.43 hrs

For Mass Balance Calculation (IPC)

Design Capacity : 2,000 m3/d

Removal Efficiency : 38% in BOD 90% in O&G 95% in TSS Treated Effluent BOD : 62% x 76 ppm = 47.12 ppm Removal BOD : 38% x 76 ppm = 28.88 ppm Treated Effluent Oil & Grease : 10% x 50 ppm = 5 ppm Removal Oil & Grease : 90% x 50 ppm = 45 ppm

Treated Effluent TSS : 5% x 1,000 ppm = 50 ppm Removal TSS : 95% x 1,000 ppm = 950 ppm

2.4.13. Clarified Water Tank

Quantity : One (1) unit Capacity : 90 m3 Dimension : ⌀ 4.6 m x 5.5 m(H) Flowrate : 83.33 m3/hr Retention Time : 90 m3 / 83.33 m3/hr = 1 hour

2.4.14. Sand Filter

Quantity : One (1) unit Dimension : ø 8.5 ft x 5 ft (SH) Pressure Rating : 50psi Flowrate : 83.33 m3/h

Design Calculation for the sizing of filter

2 2 Tank Area : AT = Q/V = 333.33 gpm / 6 gpm/ft = 55.56 ft 2 2 : AT = ∏d / 4 = 55.56 ft

Diameter of Filter, d = √[(55.56x 4) / ∏ = 8.41 ft Proposed Diameter of filter = 8.5 ft Backwash Flowrate : QBW = VBWAT = 12 gpm/ft2 x [∏(8.5)2 / 8.5] ft2 = 680.94 gpm ≈ 170.24 m3/hr

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-39

Volume of water require for backwash for 15 min. : VBW = QBW x tBW = 170.24 m3/hr x 15min = 42.56 m3

Volume of water require for rinsing for 10 min. : VBW = QBW x tBW = 170.24 m3/hr x 10min = 28.378 m3

For Mass Balance Calculation (Sand Filter)

Removal Efficiency : 60% in BOD

Treated Effluent BOD : 40% x 47 ppm = 18.8 ppm Removal BOD : 60% x 47 ppm = 28.2 ppm

2.4.15. Filtered Water Tank

Quantity : One (1) unit Capacity : 16 m3 Dimension : ⌀ 3 m x 2.73 m(H) Flowrate : 83.33 m3/hr Retention Time : 16 m3 / 83.33 m3/hr = 11.5 mins

2.4.16. Sludge Holding Tank

Quantity : One (1) unit Capacity : 150 m3 Dimension : 8.8 m(L) x 2.9 m(W) x [6 + 0.5FB] m(H)

Total Dry Sludge

BOD Sludge = 1/3 x 10,000 g/m3 x 2,000 m3/day x 1/1000 kg = 6,666.67 kg/day

TSS Sludge = 1,000 g/m3 x 2,000 m3/day x 1/1000 kg = 2,000 kg/day

Oil & Grease Sludge = 50 g/m3 x 2,000 m3/day x 1/1000 kg = 100 kg/day

Total Dry Sludge = 6,666.67 kg/day + 2,000 kg/day + 100 kg/day = 8,766.67 kg/day

*Note: The total dry sludge is calculated based on incoming parameters during average load.

Sludge Volume with = 8,766.67 kg/day 1.5% dry solid 0.015 x 1.03 x 1000 = 567.42 m3/day

Retention Time = 150 m3 / 567.42 m3/day = 6.34 hrs

2.4.17. Belt Press

Quantity : One (1) unit Type : Two Stage Type Rotary Drum Thickening Capacity : 24.5 – 41 m³/hr

Sludge Volume with = 567.42 m3/day 1.5% dry solid (after belt press)

Sludge Volume with = 8,766.67 m3/day__ 25% dry solid 0.25 x 1.15 x 1000 = 30.49 m3/day ______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-40

Weight of sludge with = 30.49 m3/day x 1.15 MT/m3 25% dry solid (after belt press) = 35.0635 MT/day = 35,063.5 kg/day

Filtrate from Belt Press: Filtrate Capacity = Sludge volume feed –cake volume = 567.42 m3/day – 30.49 m3/day = 536.93 m3/day

Solid Produced = Total sludge feed to BP – Total in BP* = 8,766.67 kg/day – 8,328.34 kg/day = 438.33 kg/day

* (Sludge captured in belt press is 95% (table 12-33, Metcalf & Eddy, 1991 Page 892)

The selected belt press capacity: 24.5 – 41 m3/hr If the capacity: 32.75 m3/hr (average capacity of belt press) Therefore, the operating hour for the belt press / day = 567.42 m3/day / 32.75 m3/hr = 17.3 hours

2.4.18. Filtrate Sump

Quantity : One (1) unit Capacity : 5 m3 Dimension : 2 m(L) x 2 m(W) x 2 m(Dp) Flowrate : 536.93 m3/day = 22.37 m3/hr Retention Time : 5 m3 / 22.37 m3/hr = 13.4 mins

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-41

2.5. MONITORING OF LTP PERFORMANCE

Monitoring of the performance of the leachate treatment plant shall be conducted regularly as follows:

Frequency of Parameter Method of monitoring Setting Monitoring

1. Incoming Influent pH Meter / pH 1.1 Influent pH Continuously pH 7 Indication Paper

Samples sent to COD ≤ 15,000 1.2 Influent COD, BOD Monthly Accredited Laboratory BOD ≤ 10,000

Samples sent to SS ≤ 50 1.3 Influent SS, O&G Monthly Accredited Laboratory O&G ≤ 1,000

2. Biological Treatment 2.1 Anaerobic MBBR 2.1.1 pH Daily pH meter pH: 6.5 - 7.5

2.2 Primary Clarifier Visual Check on clarity 2.2.1 Supernatant Daily Clear of clarified water.

2.3 Moving Bed Biofilm reactor (MBBR) 2.3.1 DO (Tank 1/2/3) Daily DO meter DO > 2.0ppm 2.3.2 pH (Tank 3) Daily pH meter pH: 6.5 - 7.5

2.4 Activated Sludge Process

(ASP) 2.4.1 pH Daily pH meter pH: 6.5 - 7.5 2.4.2 SV30 Daily Measuring tubes SV30 : 25% - 35% 2.4.3 DO Daily (if required) DO meter DO > 3.0ppm Samples send to 2.4.4 MLSS Monthly MLSS : 3000 – 4000 ppm Accredited Laboratory

2.5 Biological Clarifier Visual Check on clarity 2.5.1 Supernatant Daily Clear of clarified water. 2.5.2 pH Daily pH meter pH: 6.5 - 7.5

3. Chemical Treatment 3.1 pH Daily pH meter pH: 9.0

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-42

Frequency of Parameter Method of monitoring Setting Monitoring 3.2 Flocs (Flocculation) Daily Jar Test Big flocs

4. Sand Filter 4.1 Differential

Pressure Daily Pressure Gauge 10 psi (for backwash

monitoring)

5. Filtered Water Tank 5.4.1 pH Real-Time pH meter pH: 6.0 - 9.0 5.4.2 COD Real-Time COD Analyzer COD < 400ppm 5.4.3 A-N Real-Time A-N Analyzer A-N < 5.0ppm

6. Belt Press 6.1 Ongoing pressure Daily Pressure Gauge < 30 kPa

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-43

2.6. Design Drawings

The relevant engineering drawings for the proposed LTP is as tabulated below:-

NO. DRAWING TITLE DRAWING NO. REV

1 SITE LAYOUT PLAN PLB/LTP/SP-01 0

2 PLANT LAYOUT PLAN PLB/LTP/LAP-01 0

3 PROCESS FLOW AND P & ID DRAWING PLB/LTP/PF&PID-01 0

4 MASS BALANCE DIAGRAM PLB/LTP/MBD-01 0

5 HYDRAULIC PROFILE PLB/LTP/PFDCS-01 0

6 PERFORMANCE MONITORING CHART PLB/LTP/PMC-01 0

The Site Layout Plan included in the engineering drawings pack has shown the location where the LTP is sited within the Phase 3 Sanitary Landfill development. It is basically sited next to the proposed raw leachate collection pond (which shall be designed and constructed by others). The plot size for the LTP shall be about 1,800m2. The Site Layout Plan has also shown the final discharge location “X”, which has a geographical coordinate of 5˚11’39.5” Northing and 100˚25’29.6” Easting.

The plant facilities and processing units is shown in the Layout Plan, Altogether there are 23 on-site processing units or facilities for the LTP. In additional to that, there shall be one off-site facility of surface aerators (2 nos.) or ejectors to be installed at the inlet of the LTP system within the raw leachate pond.

The processing units have been arranged and planned in such a way that the pre-treatment, anaerobic, aerobic and anoxic treatment are located on the left side of the LTP, and the chemical- physical treatment is located on the right side of the LTP. This shall provide flexibility in the construction and operation of the LTP.

The process flow of the LTP has been depicted in the process flow diagram with plumbing and instrumentation requirements have been shown on the same diagram. The process flow diagrams have demonstrated the process sequence and pumps required to advance or return the liquid or solid to and from various processing units.

The mass balance of targeted pollutants for treatment has been captured in the mass balance diagram. It must be noted the targeted pollutants shall be largely grouped in 2 groups. The first group shall be treated in the pre-treatment, and biological treatment (An-MBBR + Primary Clarifier + MBBR + ASP + Degassing + Biological Clarifier) processes. These include BOD, COD, TSS, O&G and A-N (ammoniacal nitrogen). The second group of the pollutants shall be treated by the coagulation & flocculation process units, including oxidation reduction and decolorisation. These include copper, manganese, boron, iron, phenol, sulphide, fluoride, formaldehyde, and colour.

The hydraulic profile plan of the processing units shows levels of tank inverts and depths to demonstrate the hydraulic flow of the treatment process, either by pumping or by gravitational flow.

The performance monitoring chart is attached to demonstrate parameters to be monitored as described in Section 2.5.

The engineering drawings (A3 size) for the above have been included in Appendix 2-4.

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-44

2.7. TECHNICAL SPECIFICATION AND SCOPE OF SUPPLY

Industrial Water Engineers (M) Sdn. Bhd.’s scope of work and supply (where applicable) include consultancy, design, equipment supply, supervision of installation works, testing and commissioning of the Leachate Treatment Plant.

2.7.1. Tanks / RC and Structural Works Specifications

Item Description Quantity

Anaerobic MBBR Tank 1 / 2 1. Capacity : 380 m3 2 units Material : Alloy Steel

Safety Valve Tank 1 / 2 2. Capacity : 0.1 m3 2 units Material : SS

Primary Clarifier c/w Scum Sump 3. Capacity : 530 m3 / 4 m3 1 unit Material : RC

Buffer Tank 4. Capacity : 40 m3 1 unit Material : RC

MBBR Tank 1 / 2 / 3 5. Capacity : 500 m3 3 units Material : RC

ASP Tank 6. Capacity : 2,500 m3 1 unit Material : RC

Degassing Tank 7. Capacity : 30 m3 1 unit Material : RC

Biological Clarifier c/w Scum Sump 8. Capacity : 530 m3 / 4 m3 1 unit Material : RC

Clarified Water Sump 9. Capacity : 20 m3 1 unit Material : RC

Clarified Water Tank 10. Capacity : 90 m3 1 unit Material : Alloy Steel

Sludge Holding Tank 11. Capacity : 150 m3 1 unit Material : RC

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-45

Filtrate Sump 12. Capacity : 5 m3 1 unit Material : RC

Concrete Slab 13. 1 lot Remarks: piling is excluded

Roofing 14. 1 lot Material : Metal Cladding

Walkway c/w railing and staircase Material : Walkway/ Staircase - Mild Steel Epoxy 15. 1 lot Coated / RC Railing - Mild Steel Epoxy Coated

Platform for Belt Press c/w staircase and railing Material : Platform / Staircase - Mild Steel 16. 1 lot Epoxy Coated / RC Railing - Mild Steel Epoxy Coated

2.7.2. FRP / HDPE Tanks Specification

Item Description Quantity

pH Adjuster Storage Tank / Coagulant Storage Tank / Flocculant Storage Tank / Sodium Bicarbonate Storage Tank 1. Capacity : 1,000 L 4 units Type : Circular c/w loose flat cover Material : PE

Mixing Tank 1 / 2 and Flocculation Tank Capacity : 7 m3 / 20 m3 2. 1 unit Type : Rectangular c/w 3 compartments Material : FRP

Clean Water Tank Capacity : 16 m3 3. 1 unit Type : Circular, dome top, flat bottom Material : PE

2.7.3. Equipment Specification

Item Description Quantity

Sump Transfer Pump Type : Submersible Pump 1 duty, 1. Capacity : 85 m3/hr @ 1 bar 1 standby Power Rating : 5.5 kW / 3 ph / 415 V / 50 Hz Accessories : Isolation valve and check valve

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-46

Recirculation Pump Type : Self Priming Centrifugal Pump 1 duty, 2. Capacity : 170 m3/hr @ 1 bar 1 standby Power Rating : 11 kW / 3 ph / 415 V / 50 Hz Accessories : Isolation valve and check valve

MBBR Feed Pump Type : Submersible Pump 1 duty, 3. Capacity : 85 m3/hr @ 1 bar 1 standby Power Rating : 7.5 kW / 3 ph / 415 V / 50 Hz Accessories : Isolation valve and check valve

Scum Pump 1 / 2 Type : Submersible Pump c/w Level Float Switch 4. 2 duties Capacity : 10 m3/hr @ 0.8 bar Power Rating : 0.75 kW / 1 ph / 240 V / 50 Hz Accessories : Isolation valve and check valve

RAS / WAS Pump Type : Self Priming Centrifugal Pump 1 duty, 5. Capacity : 85 m3/hr @ 1 bar 1 standby Power Rating : 11 kW / 3 ph / 415 V / 50 Hz Accessories : Isolation valve and check valve

Clarified Water Transfer Pump Type : Self Priming Centrifugal Pump 1 duty, 6. Capacity : 85 m3/hr @ 1 bar 1 standby Power Rating : 11 kW / 3 ph / 415 V / 50 Hz Accessories : Isolation valve and check valve

IPC Sludge Transfer Pump Type : Air Operated Diaphragm Pump Inlet x Outlet : 2” x 2” 7. Material : Casing - Aluminium 1 duty Diaphragm – Santoprene Accessories : Isolation valve, check valve and flexible joint

Filter Feed Pump Type : Centrifugal End Suction Pump 1 duty, 8. Capacity : 85 m3/hr @ 3.5 bar 1 standby Power Rating : 15 kW / 3 ph / 415 V / 50 Hz Accessories : Isolation valve and check valve

Belt Press Feed Pump Type : Centrifugal Pump 1 duty, 9. Capacity : 13.5 m3/hr @ 1 bar 1 standby Power Rating : 1.5 kW / 3 ph / 415 V / 50 Hz Accessories : Isolation valve and check valve

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-47

Belt Cloth Cleaning Pump Type : Vertical Multistage Pump 1 duty, 10. Capacity : 16 m3/hr @ 6 bar 1 standby Power Rating : 5.5 kW / 3 ph / 415 V / 50 Hz Accessories : Isolation valve and check valve

Filtrate Pump Type : Self Priming Centrifugal Pump 11. Capacity : 20 m3/hr @ 1 bar 1 duty Power Rating : 3 kW / 3 ph / 415 V / 50 Hz Accessories : Isolation valve and check valve

pH Adjuster Dosing Pump / Coagulant Dosing Pump / Flocculant Dosing Pump / Sodium Bicarbonate Dosing Pump Type : Metering Pump Capacity : 4.6 L/min @ 5 bar 4 duties, 12. Power Rating : 0.18 kW / 3 ph / 415 V / 50 Hz 4 standbys Accessories : Installed in skid system c/w pressure relief valve, calibration column, flow indicator and isolation valve

BP Polymer Dosing Pump Type : Air Operated Diaphragm Pump Inlet x Outlet : 3/4” x 3/4” 13. Material : Casing - Aluminium 1 duty Diaphragm – Santoprene Accessories : Isolation valve, check valve and flexible joint

Anaerobic MBBR Mixer 14. Type : Side Mounted 4 duties Power Rating : 1.5kW / 3ph / 415 V / 50 Hz

ASP Aerator c/w Mixer Type : Surface Aerator c/w Mixer 15. Power Rating : Aerator – 55 kW / 3 ph / 415 V / 50 Hz 1 duty Mixer – 11 kW / 3 ph / 415 V / 50 Hz Accessories : Mooring cables and mooring anchors

Mixing Tank Mixer 1 / 2 (for RED & OXY Mixing) 16. Type : Top Mounted Mixer 2 duties Power Rating : 1.5 kW / 3ph / 415 V / 50 Hz

Flocculation Tank Mixer (for ABSORB Mixing) 17. Type : Top Mounted Mixer 1 duty Power Rating : 2.2 kW / 3ph / 415 V / 50 Hz

Sludge Tank Mixer Type : Submersible Mixer 18. 2 duties Power Rating : 2.8 kW / 3ph / 415 V / 50 Hz Accessories : Lifting davit and guiding rails

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-48

pH Adjuster Tank Mixer / Coagulant Tank Mixer / Flocculant Tank Mixer / Sodium Bicarbonate Tank Mixer 19. 4 duties Type : Side Clamped Mixer Power Rating : 0.4 kW / 3ph / 415V / 50 Hz

Primary Clarifier Scrapper / Biological Clarifier Scrapper Dimension : Ø 12 m Type : Peripheral Drive Material : Immersed Part - SS304, 20. 2 duties Bridge c/w handrail – Hot dipped Galvanized Power rating : 0.37 kW / 3ph / 415V / 50 Hz c/w : Clarified Control Panel

Inclined Plate Clarifier 21. Capacity : 85 m3/hr 1 duty Material : SS304 Body

Manual Backwash Sand Filter Avg. Flow Rate : 85 m3/hour Tank Dimensions : 8.5ft diameter x 5ft Height Type : Vertical Cylindrical Tank material : Mild Steel : Internal-blasting and 2 coat Cold Tar Epoxy Paint : External-blasting and 1 coat Epoxy Primer Design Pressure : 4 bar Opening :Manhole - Ø400mm JIS10K 22. Flange (Top) x 3 sets 1 duty Inlet & Outlet – JIS 10K Flange x 2 nos. Air Vent - Ø25mm T/E Flange x 1 no. Nozzle Plate : 12mm (thk) x 1 pc. Piping : PVC Sch 80 – 1 lot Accessories : - 5 units Butterfly Valve c/w Pneumatic Valve - Air Relief Valve - Pressure Gauge Media : 0.6-1.2mm - 1 layer (Fine Sand) 1.2-2.4mm - 1 layer (Fine Gravel) 2.4-4.8mm - 1 layer (Gravel)

Belt Press Type : Two Stage Type Rotary Drum Thickening Capacity : 9.5~ 16 m3/hr @ 1.5% s.s. Power Rating : i. Drive Motor – 1.37 kW / 3ph / 415 V / 50Hz ii. Agitator - 0.56 kW / 3ph / 415 V / 50 Hz 23. 1 duty iii. Thickener - 0.37 kW / 3ph / 415 V / 50Hz c/w : - Sub Panel - Frequency Inverter for 0.37 kW Drive Motor (1 unit) - Frequency Inverter for 1.5 kW Belt Press Feed Pump (2 units)

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-49

DAF Polymer Preparation Unit Capacity : 1,000 L/hr Power Rating : i. Conveyor - 0.18 kW / 3ph / 415 V / 50 Hz 24. 1 duty ii. Agitator x 3 units - 0.37 kW / 3ph / 415V 50 Hz c/w : Sub Panel

MBBR 1 & MBBR 2 Air Blower Type : Three Lobe Roots Type Capacity : 71 m³/min @ 0.8 bar 2 duties, 25. Power Rating : 132 kW / 3 ph / 415V / 50 Hz 1 standby Accessories : Inlet silencer, discharge silencer, safety valve, pressure gauge, built-in check valve, base plate

MBBR 3 & ASP Air Blower Type : Three Lobe Roots Type Capacity : 62 m³/min @ 0.8 bar 1 duty, 26. Power Rating : 132 kW / 3 ph / 415V / 50 Hz 1 standby Accessories : Inlet silencer, discharge silencer, safety valve, pressure gauge, built-in check valve, base plate

MBBR Bio-Carrier Type : X-Chip Volume : Anaerobic MBBR - 192 m3 MBBR 1 – 12 m3 MBBR 2 – 10.5 m3 27. 1 lot MBBR 3 – 6 m3 Country of : Germany Origin Type : Flat Face Material : Polyethylene White

MBBR Retaining Screen Made : IWE or equivalent 28. 1 lot Material : SS 304 Max. Flowrate: 100 m3/hr

MBBR & ASP Medium Bubble Diffuser Make : IWE (Malaysia) or equivalent 29. 1 lot Type : Mutag Germany Design Material : SS 304 Sch 10 Perforated Pipe

Electromagnetic Flowmeter Application : - Incoming to Anaerobic MBBR Tank 30. 4 units - RAS to MBBR Tank 1 - Final Discharge to Drain

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pH Controller c/w Chemical-Resistant Probe Make : HACH or equivalent

pH Sensor Range : pH 0 – 14 31. 1 set Operating temp.: -5 to 95°C

pH Controller Power Supply : 90-130 / 190-260 Vac, 50/60 Hz Analog Output: 0/4-20 mA DC

Level Float Switch 32. Cable Length : 3m / 7m 1 lot Accessories : Holding bracket

Control Panel Type : Floor Standing Material : Mild Steel Powder Coated Control : Auto-OFF-Man selector switch Electrical : ELCB, MCB, TOR, MC, Relays Component Wiring on : PVC cable in PVC trunking or conduit Stack where applicable Features : - Selector switches for pumps 33. 1 lot - Frequency Inverter for 132 kW MBBR 1 & MBBR 2 Air Blower (3 units) - Frequency Inverter for 132 kW MBBR 3 & ASP Air Blower (2 units) - Frequency Inverter for 11 kW Recirculation Pump (2 units) - Frequency Inverter for 11 kW RAS / WAS Pump (2 units)

Real-Time Monitoring for:

i) COD Analyzer 34 ii) Ammoniacal Nitrogen Analyzer iii) pH Meter (Digital Panel) iv) Real time monitoring data viewing facilities

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-51

APPENDIX 2-1

SAMPLING LOCATIONS OF THE LEACHATE

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-52

APPENDIX 2-2

SCIENTIFIC PUBLICATIONS OF FERRATE VI TREATMENT

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-53

APPENDIX 2-3

REX-OXY + ABSORB (FERRATE VI) SUPPLIER TECHNICAL INFO

______DEIA for the Proposed Phase 3 Development of Sanitary Landfill at Pulau Burung, Seberang Prai Selatan, Pulau Pinang PART 2-54

APPENDIX 2-4

ENGINEERING DESIGN DRAWINGS

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APPENDIX 2-5

GUIDELINES OF SPECIAL MANAGEMENT OF SCHEDULED WASTES

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