Catalysis is the increment of the rate of certain chemical reaction due to the additional of chemical substance known as catalyst.

Nanocatalyst for Sustainable Production of Biofuels and

Chemicals from Malaysia Bioresources

Y.H. Taufiq-Yap

PhD, CChem., FRSC (UK), FMIC (Msia), AMIChemE (UK)

Laboratory for Sustainable Bioenergy and Chemicals Catalysis Science and Technology Research Centre

Faculty of Science Universiti Putra Malaysia

Intro to Nanocatalysts

Catalysis is the increment of the rate of certain chemical reaction due to the additional of chemical substance known as catalyst.

Catalyst is the substance that accelerates a chemical reaction without itself being affected. It will provide the sites for the reactants to be activated and interacted together.

Nanocatalyst is a substance or material with catalytic properties that has at least nanoscale dimension, either externally or in terms of internal structures

1http://www.the-infoshop.com/report/bc21463_nanocatalysts.html

How it Work?

• Changes activation energy

• Offers an alternative reaction pathway

• New pathway requires less kinetic energy in molecular collisions

Objectives of preparation

 To produce a catalyst with:

– 100% selectivity,

– extremely high activity, – low energy consumption, – and long lifetime.

 This can be achieved only by precisely controlling the

size, shape, spatial distribution, surface composition

and electronic structure, and thermal and chemical

stability of the individual nanocomponents

Advantages and characteristics of nanocatalyst

 Overcome the issue of mass transfer limitation

 Reduce the Cost of Biodiesel Production

 High range of possible chemistries

 High density of active site

 Natural and synthetic

 High catalytic activity

 High surface area

 Reusable

Illustration demonstrating the effect of the increased surface area provided by nanostructured materials

Size and surface area

• Nanocatalyst can fit where many of the traditional catalyst will not.

• By nanocatalyst being very

small in size, this property

creates a very high surface to

volume ratio. This increase

the performance of the

catalyst since there is more

surface to react with the

reactants

Benefits of Nanocatalyst in Industry

Minimum chemical waste Improved economy

Energy efficiency

Reduced global warming Waste water treatment

Optimum feedstock utilization

Safer catalysts and reagents

Type of nanocatalysts

Carbon

• Graphite

• CNTs

• Carbon black

• Buckyball

• Fullerene

• Inorganic

nanotubes (e.g.

Tungsten &

Boron nitride)

Metal oxides

• Aluminium

• Iron

• Silver

• Titanium dioxide

• Cobalt

• Iron oxide

• Cerum oxide

• Calcium oxide

• Zinc oxide

Others

• Clays

• Quantum dots

• Catalysts can be either heterogeneous or homogeneous, depending on whether a catalyst exists in the same phase as the substrate

Preparation of Nanocatalyst

•

Common methods to prepare nanoparticles:

– Attrition method, grinding the particles with ball mill

– Pyrolysis method, thermochemical decomposition of organic

materials at high temperature in inert environment.

– Hydrothermal synthesis method, by crystalizing the substance from

high temperature aqueous solution at high vapor pressure.

– Chemical reduction method, reduction of metal salt in solution by

reducing agent.

– Electrochemical reduction method, precursor metal ions are

reduced at the cathode using a sacrificial as the metal source

– Ligand displacement method, the displacement of the ligand in the

organometallic complex.

Current Application of Nanocatalysts

Nanocatalyst for biodiesel production

Nanocatalyst for chemicals production

Nanocatalyst in biomass

gasification for syngas production

Nanocatalyst in biomass pyrolysis

for bio-oil production

Current scenarios of fossil fuel and

bio fuel production

• Fossil-based oil has been the most important energy and fuel source since the mid of nineteen century.

• But there has been growing distress about an energy crisis caused by o Potential fossil-based oil depletion since it is nonrenewable

resource.

o High petroleum prices

o The effect of gas emissions from petroleum on the environment

• The need for a better energy security and alarm about high petroleum prices guided people to look for sustainable, renewable energy to decrease the reliance on fossil fuels.

• Biomass and biofuels-based energy resources have possibility to become the main providers of energy in the next century.

Biofuel energy demand!

 It considers as an ideal fuel since it is biodegradable, sustainable, non-toxic, renewable and environmentally benign.

 Biodiesel has high oxygen content around (11%) and consequently being a fuel with high combustion properties

 It can be easily produced

• Biodiesel has lower oxidation stability than that of conventional diesel

• Biodiesel is most commonly produced from vegetable oils that may cause increase in the price of food i.e. (Food versus Fuel issue).

• Biodiesel has comparatively higher viscosity than conventional diesel

Biodiesel

Ad van tag es W ea kne ss

The chemistry of biodiesel production

Biodiesel is mono-alkyl esters of long-chain fatty acids derived from vegetable oils, waste coking oil and animal fats.

Nowadays; biodiesel is produced by:

Esterification

Transesterification

Potential Bio-resources for Biofuel

Bio Fuel

Palm fatty acid

distillate

Waste cooking oil

Microalgae

oil

Development of Nanoparticles Solid Acid and Bi- functional Catalysts for Production of Biodiesel from

Waste Cooking Oil

+

Waste cooking oil Methanol

Fe₂O₃-MnO-SO₄^2-/ZrO₂

Biodiesel

Waste oil Green Fuel

Z. Yaakob et al./Renewable and Sustainable Energy Reviews 18(2013)184–193 0

1 2 3 4 5 6 7 8 9 10

10

0.12

0.9

1.6

0.5

4.5

0.6

0.07

million ton/year

The total waste cooking oil production in

different countries

Z. Yaakob et al./Renewable and Sustainable Energy Reviews 18(2013)184–193

703 824 771

224

412 0

100 200 300 400 500 600 700 800 900

Crude palm oil

Rapes seed oil

Soybean oil WCO Yellow grease

Price ( USdollar /ton)

Average prices of selected oils used in

biodiesel production

5g of hydrate ZrOCl₂.8H₂O were dissolved in 100 ml of deionised water and 30% ammonium hydroxide solution was added to form white precipitate the pH was adjusted to ≈ 9-10. Aging for 12h filtered, washed several times until( –ve) test of chloride ion and dried for about 24 h at 120^oC

Fe(NO₃)₂^.9H₂O+Mn(NO₃)₂.4H₂O+(NH₄)₂SO₄+ Zr O(OH)₂ Fe₂O₃-MnO-SO₄/ZrO₂ Stoichiometric amount of Fe(NO₃)₃·9H₂O , Mn(NO₃)₂ ·4H₂O

and (ammonium sulphate or ammonium metatungstate was added to the solution of zironyl hydroxide the mixture was left under vigorous stirring at room temperature for 4 h.

Finally the mixture was dried at 120 ^o C for 12 h and then calcined at 600 ^o C -3h.

Catalyst Preparation of Fe

O

-MnO-SO

/ZrO

nanoparticles

Waste cooking oil + methanol +catalyst stir at 600 rpm at a selected temperature and time. Reaction was carried out using an autoclave reactor

Reaction mixture is centrifuged to separate catalyst.

And methanol is removed by evaporation

The glycerol is separated and WCOME’s was collected and further characterized

Biodiesel Production from Waste Cooking Oil

Effect of catalyst loading and methanol to oil molar ratio

92.2405 93.4771 94.7138 95.9505 97.1872

WCOME(%)

1.00 2.00

3.00 4.00

5.00

10.00 13.75 17.50 21.25 25.00

B: wt% of catalyst C : M eOH :Oil ratio

Effect of temperature and loading of catalyst

90.1055 91.8641 93.6227 95.3813 97.14

WCOME(%)

120.00 140.00

160.00 180.00

200.00

10.00 13.75 17.50 21.25 25.00

A: temperature C : M eOH :Oil ratio

Effect of temperature and methanol to oil molar ratio

Optimization of catalytic activity of Fe

O

-MnO- SO

/ZrO

nanoparticles

TEM image of Fe₂O₃-MnO-SO₄^2- /ZrO₂ nanoparticles

87.3155 89.4314 91.5474 93.6633 95.7793

WCOME(%)

120.00 140.00 160.00 180.00 200.00 1.00

2.00 3.00 4.00 5.00

A: temperature B: wt% of catalyst

Types of FAME’s

Retention time (min.) Standard

FAME’s

FMSZ-16 FAME’s

Myristate 7.287 7.317

Palmitate 8.416 8.492

Palmitoleate 8.967 8.931

Stearate 9.566 9.733

Oleate 9.633 9.873

Linoleate 9.792 10.090

Standard FAME’s

FMSZ-16-Biodiesel

GC chromatogram for standard FAME’s and WCO-

Biodiesel

Potential bio-resources for biofuel production in Malaysia

Bio Fuel

Palm fatty acid

distillate

Waste cooking oil

Microalgae

oil

Carbon solid acid nanocatalyst for esterification of PFAD to biodiesel

Indeed, Malaysia known as the second largest crude palm oil producer which producing 18.8 million metric tons a year².

Every year, over than 700,000 metric tones of PFAD has been produced only in Malaysia as a by-product from the refinery process².

Feedstock used for palm biodiesel production

Crude palm oil Degumming

Earth bleaching Deoderizing

Refined bleached

oil Palm fatty

acid distillate

[2] Mielke, T., The price outlook of palm and lauric oils and impacts from the global vegetable oil markets–A fundamental approach, Paper presented at the Palm and Lauric Oils Conference & Exhibition Price Outlook (POC), Kuala Lumpur, Malaysia, March 8–10, 2010.

Characteristics:

• Non-edible feedstock

• yellowish solid at room temperature

• FFA content >80 wt.% (etc.: palmitic acid, oleic acid, linoleic acid, myristic acid, stearic acid) and also containing a small percentage of squalene, sterols, and vitamin E [2].

Applications:

• soap industry, animal feed industry, as raw material for cosmetics industry and, pharmaceutical industry.

Fatty acid Formula Carbon structure

Composition wt.%

Myristic acid C₁₄H₂₈O₂ 14:0 1.93 Palmitic acid C₁₆H₃₂O₂ 16:0 45.68

Stearic acid C₁₈H₃₆O₂ 18:0 4.25 Oleic acid C₁₈H₃₄O₂ 18:1 40.19 Linoleic acid C₁₈H₃₂O₂ 18:2 7.90 Table. Fatty acids composition of PFAD

Fig.3:GC-MS chromatogram of PFAD

Palmitic Oleic Linoleic

[2] Ab Gapor Md Top, 2010, Production and utilization of palm fatty acid distillate (PFAD).Lipid Technology 22(1):11-13.

Palm Fatty Acid Distillate (PFAD), Physical and

Chemical Properties

Preparation of carbohydrate-derived solid acid catalysts

Calcination at 400°C for 12h with N₂ gas flow

Black powder of incomplete carbonized carbon after milling process

Washing process to remove an excess of sulphuric acid Sulfonated carbohydrate-

derived solid acid catalyst Carbohydrate

samples

Sulfonation with conc.

H²SO⁴ in N₂ gas flow at 150°C for 12h

Fig.Preparation of sulfonated-glucose catalysis: (A) pyrolisis, (B) carbonization and (C) sulfonation.

Reflux Centrifugation Purification Product

PFAD + Methanol + catalyst

Speed:

3500 x g

Time: 15 min

PFAD

methyl ester

@ Biodiesel

FAME

Methanol

Methanol recovery and washing

Hot water

Biodiesel Production from PFAD

Catalytic activity of solid acid carbon catalyst in esterification of PFAD

0

80.8

92.1 94.6 95.4 95.8

0 20 40 60 80 100

0 20 40 60 80 100

0 1 2 3 4 5

FAME yield, %

FFA conversion, %

Reaction time, h

FAME yield FFA conversion 34.6

79.2

94.7 95 95.9 96.3

0 20 40 60 80 100

1 5 10 15 20 25

FFA conversion, %

Methanol/PFAD molar ratio

12.8

85 94.9 95.1 96.7 96.5

0 20 40 60 80 100

0 1 2 3 4 5

FFA conversion, %

Catalyst amount, wt.%

85.8 88.6

94.6 94.8 94.1

50 60 70 80 90 100

65 70 75 80 85

FFA conversion, %

Reaction temperature, °C

Reusability and leaching analysis of starch-derived solid acid catalyst

Reaction Conditions Reaction

Temperature

75 °C Reaction Time 4 h Methanol-to-PFAD

Molar Ratio

13.6:1 Catalyst Loading 3.6

wt.%

• The reusability study has been conducted in order to study the stability and reusability of the catalyst.

• The Fig. presented the ability of starch-derived solid acid catalyst to reuse which was up to 5 times before the conversion is below than 80%.

• The leaching analysis revealed that the leached S from the catalyst was in the limit. (limit for S content: ASTM < 0.0015, EN < 0.0010 wt.%).

Fig. The trends of reusability of the catalyst and leaching of the S content 94.6 91.6

87.3 85.5

81.2 75.2

0

0.0005 0.001 0.0015 0.002

0 10 20 30 40 50 60 70 80 90 100

1 2 3 4 5 6

S content (ppm)

FAME yield

Reaction cycle

FFA conversion

Properties of FAME product

Properties Units Methods PFAD

biodiesel^a

ASTM D6751-02

EN 14214

Viscosity at 40°C

mm²/s ASTM D445 4.85 ± 0.03 1.9 ̶ 6.0 3.5 ̶ 5.0

Acid value Mg KOH/g ASTM D664 0.65 ± 0.01 0.80 max 0.50 max Density at 15°C Kg/m³ ASTM D4052 875 ± 2.6 870-900 860-900

Cloud point °C ASTM D2500 13.2 ± 0.17 -3 to 12 -

Moisture content

mg/kg ASTM D6304 0.03 ± 0.08 0.03 max -

Pour point °C ASTM D97 12 ± 0.21 -15 to 10 -

Flash point °C ASTM D93 178 130 min 120 min

a PFAD biodiesel in this work was produced by esterification of the PFAD using RSM optimized condition at 13.6:1 of methanol-to-PFAD molar ratio, 75°C reaction temperature, 3.6 wt.% of catalyst and 4 h reaction time.

The properties of the PFAD biodiesel produced was in the range of the ASTM D6751-02 and EN 14214 standards. Except for the pour point and cloud point was respectively slightly higher as compared to the ASTM D6751-02 standard. This is due to the highly saturated FFA in PFAD which results in high value of pour point and cloud point

Accepted for publication in Renewable Energy on

17 March 2015

Potential bio-resources for biofuel production in Malaysia

Bio Fuel

Palm fatty acid

distillate

Waste cooking oil

Microalgae

oil

Calcium Methoxide as Heterogeneous Nanocatalyst

for Transesterification of Nannochloropsis Oculata

Microalgae’s Oil to Biodiesel

Biodiesel Generation

[1]Alam, F., Date, A., Rasjidin, R., Mobin, S., Moria, H., & Baqui, A. (2012).Procedia Engineering, 49, 221-227.

[2] Li, Y., Horsman, M., Wang, B., Wu, N., & Lan, C. Q. (2008)..Applied microbiology and biotechnology, 81(4), 629-636

EDIBLE OIL

MICROALGAE OIL

Unicellular [1]

naturally found in fresh water and marine

environment [1]

capable of fixing CO₂in the atmosphere[2]

can grow rapidly [2]

NON-EDIBLE OIL

Plant source Seed oil

content (% oil by

wt. in biomass)

Oil yield (l oil/ha/year)

Land use (m²year/

kg biodiesel

)

Biodiesel productivity

(kg biodiesel/ha/year)

Jatropha (Jatropha curcasL.) 28 741 15 656

Palm oil (Elaeis guineensis) 36 5366 2 4747

Microalgae (low oil content) 30 58,700 0.2 51,927

Microalgae (medium oil content) 50 97,800 0.1 86,515

Microalgae (high oil content) 70 136,900 0.1 121,104

Why microalgae for biofuel?

High oil yield (15-300 time more oil than traditional crops Above 50 %, some as high as 75 %)

-Microalgae: 5000 to 15000 gallons/acre/year -Oil Palm: 635 gallons/acre/year

-Sunflower: 102 gallons/arce/year

Lesser land requirement: limited land resources make solved the potential biomass insufficient

Food vs fuel: does not compete with food supply

Adaptability & high growth rate: > 50 times faster than land based plant & consumes very less water compare to land crops

High CO₂ capture capacity: high photosynthesis efficiencies (CO₂convert to O₂) – algae in carbon cycle

Preparation of Ca(OCH 3 ) 2 nanoparticles

Pure metallic oxide precursor

CaO

Alcohol reagent Methanol

Formation of white slurry solid base

+

Reflux & stir at 65 ^oC for 2 – 12 hours

Remove MeOH using rotary evaporator

Dry in the Oven at 378 K for 1h

50 ml min^-1 N₂flow

Ca(OCH₃)₂

TEM images of Ca(OCH₃)₂nanoparticles

Cultivation, Extraction & Catalytic test: crude microalgae derived oil (MDO)

Biodiesel production from Algae Oil

Influence of (a) methanol ratio, (b) catalyst concentration and (c) reaction time on transesterification of extracted N. oculata lipid from dried microalgae: catalyst dosage 3 % (a), reaction time 3 h (a, b), reaction temperature 60^oC (a, b).

0 10 20 30 40 50 60 70 80 90 100

10 20 30 40 50 60

FAME yield (%)

MeOH ratio (%) 6.95

0 10 20 30 40 50 60 70 80 90 100

0 3 6 9 12 15

FAME yield (%)

Catalyst loading (%)

0 10 20 30 40 50 60 70 80 90 100

0 0.5 1 1.5 2 2.5 3 3.5 4

FAME yield (%)

Reaction time (h)

Ca(OCH3)2 CaO NaOH

Transesterfication condition: reaction temperature of 60^oC, 12 wt. % of catalyst and methanol/oil ratio of 30:1.

Transesterfication condition: reaction temperature of 60^oC, 4 wt. % of catalyst and methanol/oil ratio of 30:1.

Transesterfication condition: reaction temperature of 60^oC, 3 wt. % (1 mol) of catalyst and methanol/oil ratio of 12:1.

13.79

14.04 17.83

30.57

85.44

1.57

60.11

83.60

61.56 92.02

13.79

97.60 92.00

83.02 87.46

82.16 85.53

63.17 73.55

(a) (b)

(c)

Catalytic Activity

0 20 40 60 80 100

1 run 2 run 3 run 4 run 5 run 6 run

FAME yield (%)

Run times

0 5 10 15 20 25 30 35 40

C14:0 C16:0 C18:0 C16:1 C18:1 C18:2 C:20:4 C20:5 C22:6

Concentration (%)

Fatty acid methyl ester profile

FAME yield > 90 %

35.43 %

27.54 %

Unsaturated FAME > 50 %

Methyl ester Carbon Methyl laurate C 12:0 Methyl myristate C 14:1 Methyl palmitate C 16:0 Methyl palmitoleate C 16:1 Methyl stearate C 18:0 Methyl oleate C 18:1 Methyl linoleate C 18:2 Methyl arachidate C 20:0 Methyl docosanoate C 22:0

All cis 5,8,11,14,17- methyl eicosapentenoate

C 20:5(n3)

Reusability

Malaysia generates 80 m tonnes of dry palm biomass per year

Annual availability

9.6 46.4

0.8 4.1

1.4 6.7

1.4 6.9

3.0 Per ha

(tonnes of dry biomass)

National total (m tonnes of dry biomass) Site of

production Plantation

Mill Mill

Mill

Plantation 14.4

Biomass Type

Shells (PKS) EFB

Empty Fruit Bunch

Fiber

Mesocarp fibre

Fronds

Trunks

12.2 (wet weight)

59.3 (wet weight)

POME Mill

Palm Oil Mill Effluent

Biogas from Palm Oil Mill Effluent (POME)

• About 0.65 – 0.675 m³of POME is generated for every 1 tonne of FFB processed

• 56 million tonnes of POME generated in 2009

• Biogas is produced during the decomposition of organic matters in anaerobic pond

• It contains about 60-70 % Methane (CH₄), 30-40 % Carbon Dioxide (CO₂) and trace amount of Hydrogen Sulphide, (H₂S)

• Methane - the global warming potential – 21 times higher than CO₂

• Potential yield: 1 m³of completely digested POME produces 28 -38 m³ biogas

• 1624 million m³ of biogas generated in 2009

• GHG emission reduction: 16 – 20 million tonnes CO2 eq.

CO

CH

CH

CO

CH

Trapping of Biogas at Palm Oil Mills

• Under National Key Economic Areas (NKEA) – palm oil sector: all palm oil mills to have biogas trapping

facilities by 2020

• 16 – 20 million tonnes of carbon dioxide equivalent per year

mitigated

Biogas Plant at Palm Oil Mills

• Two technologies: digester and covered lagoon

•Biogas application:

- Electricity generation - on & off grid - CHP - steam and heat

- Co-firing in biomass boiler and diesel genset to reduce the utilization of the palm shell and diesel

• Power potential: 1 -2 MW from 60 t/hr POM

Ponding system of POME treatment

Bell Eco Power Sdn. Bhd., Batu Pahat

Biogas Capture from POME

Electricity Generation from Biogas

– 1

Grid-Connected Biogas Plant (1.7 MW)

National Key Economic Areas (NKEA)

NATIONAL BIOGAS IMPLEMENTATION (EPP5)

To produce hydrogen

Biogas

Production: 28m³/m³ POME Composition

CH₄ : 62.5 % CO₂ : 37 %

H₂S : 150-200 ppm

CH 4 + CO 2 2CO + 2H 2

Dry Reforming of Biogas

Catalyst:

Noble metal catalysts:

Pt, Ru and Rh - high activity and more resistant to coke formation but very expensive and limited availability.

Ni-based catalysts:

- more suitable,

- high activity, availability and low price.

- but more sensitive to carbon deposition and difficult to prevent

sintering of nickel.

Fig. 7: XRD pattern of reduced catalysts

• XRD patterns showed that Ni metallic phase formed after reduction process

• The Ni particles are relatively small of around 13-15 nm. The differences are due to the

different method used

Ni/CS-S Ni/CS-D

NiCo/CS-D NiPt/CS-D Sample CeO₂^a

(nm)

NiO^b (nm)

Ni^c (nm) Ni/CS-S 8.07 10.63 14.96 Ni/CS-D 5.53 8.94 13.39 NiCo/CS-S 7.16 9.30 14.85 NiCo/CS-D 5.47 8.03 12.75

NiPt/CS-D 6.08 9.80 12.82 Fig. 8: TEM images of selected reduced catalysts Table 2: Crystalline particle size

20 30 40 50 60 70 80

Ni JCPDS 004-0850 CeO₂ JCPDS 043-1002

NiPt/CS-D





 = SiO₂

 = CeO₂

 = Ni









NiCo/CS-D

Ni/CS-D NiCo/CS-S

Ni/CS-S

2 (degree)

Intensity (a.u.)

Crystallographic & Particle sizes

52

NiCo/CS-S

40 50 60 70 80 90 100

0 100 200 300 400 500 600

CO2Conversion(%)

Time on stream (min

Ni/CS-S Ni/CS-D NiCo/CS-S NiCo/CS-D

40 50 60 70 80 90 100

0 100 200 300 400 500 600

CH4Conversion (%)

Time on stream (min)

Ni/CS-S Ni/CS-D NiCo/CS-S NiCo/CS-D NiPt/CS-D

Catalytic performance of catalysts as a function of time at GHSV 3000 ml/g

.h

(a) CH

conversion and (b) CO

conversion

a b

Catalytic Evaluation

53

Catalyst activities over all catalysts

TGA profiles of spent catalysts The spent catalysts

• Catalyst prepared by sequenced method showed lower amount of mass loss, indicating lower carbon formation

• NiPt/CS-D gave low carbon formation due to the existence of Pt Carbon formation analysis: TGA

54

20 30 40 50 60 70 80 90 100

50 150 250 350 450 550 650 750 850

Mass loss (%)

Temp (^oC)

Ni/CS-S Ni/CS-D NiCo/CS-S NiCo/CS-D NiPt/CS-D

Carbon formation analysis: SEM

55

SEM images of spent catalysts

Gasification

Air, heat, water & catalyst

Ash, Char & liquids

Gases to Fischer- Tropsch process:

H₂, CO, CO₂, CH₄, C₂H₂, C₂H₄

Biomass feedstock

SNG - substitute Natural Gas; MTO – methanol to Olefin; MTG – methanol to gasoline

Postgraduate Students

• PhD

Theam Kok Leong Teo Siow Hwa

Sivasangar Seenivasagam Mohd. Lokman Ibrahim Mohd Sufri Matuli

Nurul Suziana Nawi Faris Jasim

• MSc

Surahim Rabiah

Lai Fook How Ivan Tan

Rachel Tang Duo Yao Davin Yap

Ezzah Mahmudah Arfaezah

Abdul Kareem al Sultan

Graduated Students

1. Dr. Tan Kian Peng (Metalysis Ltd., UK) 2. Dr. Looi Ming Hoong (UM)

3. Dr. Leong Loong Kong (UTAR)

4. Dr. Goh Chee Keong (Republic Polytech, Singapore) 5. Dr. Ali Asghar Rownaghi (Georgia, USA)

6. Dr. Tang Wen Jiunn(KDU)

7. Dr. Wong Yee Ching(UM Kelantan) 8. Dr. Lee Hwei Voon(UM)

9. Dr. Fath Elrahman Hamid (Sudan)

10. Dr. Mohd. Hasbi Abdul Rahim (UM Pahang) 11. Mr. Saw Chaing Sen (INTEL Malaysia)

12. Mr. Ahmad Raslan Mat Hussin (Bernas) 13. Ms. Ita Jong (Canada)

14. Mr. Peh Tian Hai (ICI) 15. Dr. Lim Gin Keat (USM) 16. Dr. Nor Asrina Sairi (UM) 17. Mr. Theam Kok Leong (UTAR) 18. Ms. Nurul Fitriyah Abdullah

19. Mr. Tang Lok Hing (Republic Polytech, Singapore) 20. Sudarno (Indonesia)

21. Asiah Abdullah (UiTM) 22. Suhaizam Suhaimi (UIA) 23. Yuen Choon Seong

24. Aqilah Noor 25. Shajaratunnur 26. Nur Faizal

27. Nur Asikin Mijan

THANK YOU TERIMA KASIH

ありがとうございました 감사

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