FINAL YEAR PLANT DESIGN I

GROUP FYDP 8

PRODUCTION OF METHANOL AND ACETIC ACID

GOH WAI BOON 11120 MUHAMMAD 'IMRAN BIN ISHAK 11165 NOR RALINA BINTI KAMALUDDIN 11176 NURUL HAYATI BINTI AHMAD 11791 LEENA YEAWAE 10513 MUHAMMAD ZUBAIR BIN GHAZALI 11789

Introduction Literature Review

- Product Market Survey

- Plant location

Preliminary Hazard Analysis Conceptual Design Economic Potential Mass Balance Calculation Preliminary Heat Integration Process Flow Sheet Recommendations Conclusions

PRESENTATION CONTENTS

INTRODUCTION

70,000 MT/yr of methanol per year and 60,000 MT/year of acetic acid

95% purity by mole and excess water Conform to all Malaysian environmental laws Adhere to all Malaysian safety regulations. Recover and reuse process materials Minimize energy consumption

PROBLEM STATEMENT

OBJECTIVES OF FYDP

• To conduct literature survey, this includes the main product acetic acid

whereby all the process routes, properties, uses and market cost.

• To identify the best process route for the plant design project.

• To develop the best process flow sheet for the selected chemical process

• To develop and calculate the energy balance and complete material.

OBJECTIVES OF PROJECT

•To design a profitable methanol and acetic acid manufacturing plant in Malaysia.

•To meet the increasing demands of acetic acid the market.

SCOPE OF WORK

A. Conduct literature review

B. Generate process flow sheet (PFD)

C. Calculate Material and Energy Balances (MEB)

D. Estimate pre-design cost (Economic potential)

E. Simulate (iCON)

F. Preliminary heat integration

G. Preliminary Hazard Analysis

METHANOL

Methanol Overview

Methanol

CH3OH

light., volatile , colorless

Flammable liquid with a

distinctive odor

Burn to form carbon dioxide

and steamOxidized to

form formaldehyde

Polar liquid at room

temperature

ACETIC ACID

Acetic Acid Overview

Acetic Acid

CH3COOH

Colorless liquid, pungent odor

Miscible with water in all proportions

Corrosive and attack the skin

A weak acid

LITERATURE REVIEW• Product Market Study

• Site Feasibility Study

PRODUCT MARKET SURVEY

Location Production (2010) Consumption(2010)

Asia 19.11 25.44

North America 0.98 7.20

South America 10.29 0.96

Europe 3.43 9.12

Middle East 9.80 2.88

Other 5.39 2.40

Total 49.00 48.00

Production, and Consumption for Methanol, 106 t/ year

Location Production (2010) Consumption (2010)

Asia 10.00 5.99

North America 2.92 2.10

South America 0.92 0.96

Europe 0.30 1.47

Middle East 0.50 0.08

Other 1.30 0.24

Total 15.39 10.50

Production, and Consumption for Acetic Acid, 106 t/ year

PRODUCT MARKET SURVEY

World Consumption for Methanol and Acetic Acid

Raw Materials Price

Natural gas, coal as well as biomass (wood chips).

(A) Natural Gas Natural gas price = RM 13.70/MMBtu

(B) Coal

Currency 1 USD = RM 3.125*Coal price = USD 130/tonne = RM 406.25/1000 kg = RM 0.4063/kg

(C) Wood Chips

Biomass (Wood Chips) price = RM 250/metric tonne = RM 0.25/kg

Products Price

(A) Methanol

Currency 1 USD = RM 3.125*Methanol price = USD 470/MT

= RM 1468.75/MT

(B) Acetic Acid

Currency 1 USD = RM 3.125*Acetic Acid = USD 540/tonne

= RM 1687.5/tonne

Factors in site selection :

i. Raw Materials Availability

ii. Marketability

iii. Utilities

iv. Land Available and Cost

v. Transportation Facilities

vi. Waste Disposal

vii. Labor Supply

viii. Taxation and Legal Restrictions

ix. Government Incentives

SITE FEASIBILITY STUDY

SITE SURVEY

GEBENG INDUSTRIAL AREA,PAHANG

KIDURONG INDUSTRIAL AREA,SARAWAK

PAKA INDUSTRIAL AREA,TERENGGANU

RECOMMENDED AREA

MAP OF PASIR GUDANG,JOHOR

TELUK KALUNG INDUSTRIAL AREA,KEMAMAN,TERENGGANU

Factors

Site Location

Gebeng Industrial

Area, Kuantan, Pahang

Kidurong Industrial

Area, Bintulu, Sarawak

Paka Industrial

Area, Dungun,

Terengganu

Pasir Gudang

Industrial Area, Johor

Teluk Kalong

Industrial Area,

Kemaman, Terengganu

Type of Industrial Area 9 5 9 6 7Raw Materials Methane 2 1 6 3 4

Utilities

Power 8 5 8 7 8Water 6 6 8 8 9Steam 10 3 10 3 8

Natural Gas 5 10 10 3 7

Available Area 10 5 4 1 7Land Price 4 5 8 1 8

Space for Expansion 9 5 5 2 5Cost of Living 5 8 8 2 8

Transportation

Seaport 10 10 8 10 10Railway 9 6 9 7 9Roadway 7 6 8 8 8Airport 10 10 8 8 10

Price of Utilities Power 7 8 7 7 7Water 9 8 5 7 5

Existing Infrastructure 10 10 10 10 10Existing Services for Industrial

Accidents 10 10 10 10 10

Training Centre 8 0 10 5 10Government Incentives 7 7 7 7 7

TOTAL SCORE 155/ 200 128 / 200 158 / 200 115 / 200 156 / 200PERCENTAGE (%) 77.5 % 64.0 % 79.0 % 57.5 % 78.0 %

RANKING 3 4 1 5 2

Paka Industrial Area, Dungun

a) Ready built industrial land for heavy industries.b) The raw materials which is the methane can easily be

obtained from PETRONAS Gas Berhad (PGB).c) Centralized Utilities and Facilities (CUF) at Kerteh.d) Existence of all major transportation networkse) Strategically located in the heart of South East Asia,

f) Economical local manpower g) Strong institutional support from government department

and local authority

SELECTED AREA

PRELIMINARY HAZARD ANALYSIS

Type Chemicals/Materials

Feed Methanol

Natural gas

- Methane (CH4)

- Ethane (C2H6)

- Propane (C3H8)

- Carbon dioxide (CO2)

- Nitrogen (N2)

Water (H20)

Acetic acid

Methanol (CH3OH)

Carbon monoxide (CO)

Intermediate Product Methanol process

Hydrogen (H2)

Carbon monoxide (CO)

Acetic acid process

Methanol (CH3OH)

Hydrogen (H2)

Carbon monoxide (CO)

Product Methanol acetic acid

Byproduct Methanol process

DME,higher alcohols,minor amount of acid and aldehydes

Acetic acid process

N2,H2,CO2,CH4,hydrogen iodide,formic acid, hydrogen sulfide

(H2S),Water,proionic.

Solvent Methanol

Amine based

Acetic acid

Acetic acid

IDENTIFICATION OF CHEMICALS

Occurrence Methods

Exposure to methanol Avoid prolonged or repeated breathing of methanol vapor.

Proper ventilation to ensure safe working conditions.

Breathe in methanol Remove contaminated clothing, wash with soap and water for 15

minutes.

In case of inhalation of methanol vapor, remove the individual to fresh

air.

Spill of methanol Stop or reduce discharge of material if this can be done without risk.

Isolate the spill or leak area immediately for at least 330 to 660 feet in

all direction.

Eliminate all sources of ignition, and stay upwind.

Prevent methanol from entering into waterways, sewers, basements or

confined area.

Fire start around methanol Accumulations of methanol vapors in confined spaces may explode if

ignited.

Keep open flames, sparks and oxidants away from methanol.

Handling Methanol

Occurrence Methods

Store of methanol Methanol should always be kept within closed systems or approved containers and never left open to the atmosphere.

Containers should be labeled in accordance with local regulations and site requirements.

Materials and methods of construction must be compatible with methanol service.

Disposal of excess methanol Large quantities of waste methanol can either be disposed of at licensed waste solvent company or reclaimed by filtration and distillation.

Waste methanol, or water contaminated with methanol, must never be discharged directly in sewers or surface waters.

Handling Methanol

LOCAL SAFETY REGULATIONS

The following is the related act of OSHA for the process plant safety:

•Factories and Machinery Act 1967

•Occupational Safety and Health (The Control of Industrial Major Accident Hazards) Regulations 1996

•Occupational Safety and Health (Classification, Packaging, and Labeling of Hazardous Chemicals) Regulations 1997

•Occupational Safety and Health (Use and Standards of Exposure of Chemicals Hazardous to Health) Regulations 2000

Occupational Safety and Health Act (OSHA) 1994

CONCEPTUAL DESIGN

Criterions used to choose a catalyst :

• Activity

• Stability Environmental requirements

• Maximum conversion and selectivity

• High throughput

• Minimum Process Cost

Catalyst available for the process :

• Metals such rhodium or iridium (Acetic acid)

• Nickel (SMR)

CATALYST SELECTION

Rhodium (ACETICA Process)

CATALYST SELECTION

The amount of catalyst in the reactor can be raised without

the solubility limitations

The loss of expensive rhodium by precipitation can be lowered

High product output with minimal byproduct production Provides 85% conversion with 99.8% selectivity of

methanol. Catalyst can last for 3 months

Nickel (SMR)

CATALYST SELECTION

Type of Reactor Characteristics Uses Advantages Disadvantages

CSTR Run at steady state with

continuous flow of

reactants and products; the

feed assumes a uniform

composition throughout the

reactor, exit stream has the

same composition as in the

tank

Kinds of Phases Present

-Liquid phase

-Gas-liquid reactions

-Solid-liquid reactions

-When agitation is required

-Series configurations for

different concentration

streams

-Continuous operation

- Good temperature control

-Easily adapts to two phase

runs

-Good control

-.Simplicity of construction

-Low operating (labor) cost

-Easy to clean

-Lowest conversion per unit

volume

-By-passing and channeling

possible with poor agitation

PFR Arranged as one long

reactor or many short

reactors in a tube bank ; no

radial variation in reaction

rate (concentration);

concentration changes with

length down the reactor

Kinds of Phases Present

-Primarily Gas Phase

-Large Scale

-Fast Reactions

-Homogeneous Reactions

-Heterogeneous Reactions

-Continuous Production

-High Temperature

-High Conversion per Unit

Volume

-Low operating (labor)

cost)

-Continuous Operation

-Good heat transfer

- Undesired thermal

gradients may exist

-Poor temperature control

-Shutdown and cleaning

may be expensive

SELECTION OF REACTOR

Type of Reactor Characteristics Uses Advantages Disadvantages

Fixed-Bed reactor

( Multi-tubular

Reactors)

-Types of reactors

are modified

multiple fixed-bed

units, where the

multiple beds are

catalyst-filled tubes

arranged in parallel

with a heat

conducting fluid

flowing outside the

tubes.

Kinds of Phases Present

-Gas phase/ solid

catalyzed

-Gas-solid reactions

-Used primarily in

heterogeneous has phase

reactions with a catalyst

-Oxidation of ethylene to

ethylene oxide

-Hydration of propene to

isopropanol.

-temperature control

with liquid and gaseous

-heat transfer agent in

shell-side

-These reactors offer

good thermal control and

uniform residence time

distribution

-High production rates

and conversion per unit

volume

-Low operating cost

-This reactor will require

a high cost in shutdown

and cleaning the reactor.

-long downtime for

catalyst replacement

-large pressure drop

-distribution devices

needed for stream of

reaction gas in large

reactor

SELECTION OF REACTOR

Type of Reactor Characteristics Uses Advantages Disadvantages

Fluidized-bed -Analogous to CSTR

Cannot be modeled as

either a CSTR or a

tubular reactor (PFR)

Fluid flow from

bottom of reactor to

the top causing small

particles (packing) to

be suspended

-Gas-solid phase

reaction that requires

large interfacial

surface to react

-catalytic cracking of

petroleum naphtha to

form gasoline

-The temperature is

relatively uniform

throughout the bed

-It doesn’t have hot

spot

-Good temperature

control

-Can handle large

amounts of feed and

solid

-Ease in catalyst

replacement

-High cost of the

reactor and catalyst

regeneration

equipment

-Under certain upset

conditions, catalysts

stickiness occurs.

-Because of the

inherent back-mixing,

it is not possible to

achieve total

conversion of the

stoichiometric

limiting feed

-Requires much more

catalyst for high gas

conversion and

greatly depress the

amount of

intermediate, which

can be formed in

series reaction.

MASS BALANCE CALCULATIONS

METHANOL

COMPONENT

Stream 3 form (manual)

(kmol/hr)

Inlet

T = 302 K , P = 20 atm

Stream 3 from (ICON)

(kmol/hr)

Inlet

T=302 K, P=20 atm

Variance(%) difference between

manual and ICON

Methane 306.471 306.471 0

Ethane 13.464 13.464 0

Propane 2.541 2.541 0

Hydrogen 0 0 0

Carbon monoxide 0 0 0

Carbon dioxide 6.039 6.039 0

Nitrogen 1.485 1.485 0

Water 990 990 0

Total 1320 1320 0

METHANOL

COMPONENT

Stream 4 from (manual)

(kmol/hr)

Outlet

T= 1143 K, P = 20 atm

Stream 4 from (ICON)

(kmol/hr)

Outlet

T=1143 K, P=20 atm

Variance(%) difference between

manual and ICON

Methane 56.82 56.82 0

Ethane 0 0 0

Propane 0 0 0

Hydrogen 948.310 948.310 0

Carbon monoxide 169.953 169.953 0

Carbon dioxide 120.288 120.288 0

Nitrogen 1.485 1.485 0

Water 585.51 585.51 0

Total 1882.366 1882.366 0

METHANOL

COMPONENT Stream 24 from (manual)

(kmol/hr)

Inlet

T= 461 K, P = 20 atm

Stream 24 from (ICON)

(kmol/hr)

Inlet

T=461 K, P=20 atm

Variance(%) difference between

manual and ICON

Methanol 0 0 0

Carbon monoxide 69.000 69.001 0.0015

Water 0 0 0

Acetic Acid 0 0 0

Ethyl Acetate 0 0 0

ACETIC ACID

COMPONENT Stream 25 (from manual)

(kmol/hr)

Outlet

T= 454.9 K, P = 0.29 atm

Stream 25 from (ICON)

(kmol/hr)

Outlet

T=454.9 K, P=0.29 atm

Variance(%) difference between

manual and ICON

Methanol 3.853 3.851 0.052

Carbon monoxide 3.436 3.444 0.233

Water 123.235 123.230 0.004

Acetic Acid 147.875 147.871 0.002

Ethyl Acetate 0 0 0

ACETIC ACID

ECONOMIC

POTENTIAL

Level 1 Economic Potential (EP1)

Different single pass conversion based on same catalyst :

Temperature(oC)

Single pass conversion,%

Conversion,%

Methanol

1 248.85 35.0 35.0

CH4 + H2O → CH3OH + H2

Methane Methanol

Level 1 Economic Potential (EP1)

Different single pass conversion based on same catalyst :

CH3OH + CO → CH3COOH

Methanol Acetic Acid

Temperature(oC)

Single pass conversion,%

Conversion,%

Acetic Acid

1 248.85 54.5 54.5

Level 2 Economic Potential (EP2)

Natural Gas to Methanol

The price of methanol over a period of 7920 operating hours is:

The cost of natural gas over a period of 7920 operating hours is:

Thus, economic potential at level 2 is:

Methanol to Acetic Acid

The price of acetic acid over a period of 7920 operating hours is:

The cost of methanol over a period of 7920 operating hours is:

Level 2 Economic Potential (EP2)

The price of methanol for production over a period of 7920 operating hours is:

Thus, economic potential at level 2 is:

Level 3 Economic Potential (EP3) 

Natural Gas to Methanol

At Level 3, Economic Potential 3 is obtained from the following:

Methanol to Acetic Acid

At Level 3, Economic Potential 3 is obtained from the following:

Level 3 Economic Potential (EP3)

HEAT INTEGRATION

ADVANTAGES AND DISADVANTAGES

Advantages Disadvantages

Integrated

Cooling and heating utility is decreased.

Extra units of heat exchanger need to be installed-installation

costs needed.

Saving of cold and hot utility - Cost savings.

Hot streams are kept hot and cold streams are kept cold.

Offers trade-off between energy usage with capital costs.

Degree of freedom become less, therefore complex control

systems are needed, to decrease disturbances.

METHANOL

Stream TypeT supply

(°C)T target

(°C) DT DH (KCAL/HR) DH (KW) FCp (KW/°C)

S4-S5 Hot 869.85 96.85 773 -54658000 -63523.22394 82.17752127

S9-S10 Hot 249.85 24.85 225 -18333000 -21306.51075 94.69560333

S14-S15 Cold 9.85 145.85 -136 14243000 16553.13547 121.7142314

Condenser T-12 Hot 81.98 -172.57 254.55 -1.67E+07 -19357.97554 76.04783164

Reboiler T-12 Cold 175.43 178.01 -2.58 1.73E+07 20154.4274 7811.793565

Condenser T-14 Hot 99 98.99 0.01 -7.39E+07 -85943.00075 8594300.075

Reboiler T-14 Cold 103.57 125.9 -22.33 6.51E+07 75627.71152 3386.820937

Summary of The Hot and Cold Stream Available For Heat Integration

METHANOLDesign Above Pinch

Minimum Heating Utility = 5146.0777 + 20154.4274 + 573.378911= 25873.88kW

Minimum number of utilities = Number of streams + number of utilities - 1 5 + 3 - 1 = 7

METHANOLBelow Above Pinch

Minimum Cooling Utility = 1374.0082 + 8401.3939 + 7950.9178 + 85943.001

=103669.32 kW

Minimum number of utilities = Number of streams + number of utilities - 1 5 + 4 - 1 = 8

METHANOL

UtilitiesBefore Integration

(kW)

After Integration

(kW)

Energy Saved

(kW)

Hot 190000 25873.88 164126.12

Cold 112000 103669.32 8330.68

Comparison Between Utilities Consumption Before And After Minimum Energy Recovery

In this plant, after the heat integration, the energy saving is concluded below.

Temperature – Interval Heat Balance

ACETIC ACID

HOT STREAMS

UNIT TYPETsupply

(K)Ttarget

(K) TF

(kgmol/hr)H

(MW)FCp

(MW/K)

Cp(kJ/

kgmol.K)

X5 HOT 573.15 473.15 -100.00 4588.95 -4.767 0.047 36.87

X7 HOT 473.15 423.15 -50.00 4444.46 -2.291 0.046 37.26

C1 HOT 500.00 323.15 -176.85 1103.36 -15.150 0.086 280.60

C2 HOT 418.77 303.15 -105.62 270.16 -1.420 0.013 173.23

C3 HOT 503.61 323.15 -180.46 833.20 -13.067 0.072 311.09

Total H   -36.695

COLD STREAM

UNIT TYPETsupply

(K)Ttarget

(K) TF

(kgmol/hr)H

(MW)FCp

(MW/K)

Cp(kJ/

kgmol.K)

R4 COLD 357.00 573.15 216.15 4587.43 9.903 0.046 35.88

          Total H   9.903  

Summary of The Hot and Cold Stream Available For Heat Integration

ACETIC ACIDAbove Pinch Design

ACETIC ACIDBelow Pinch Design

ACETIC ACID

Utility TypeBefore MER

(MW)

After MER

(MW)

Energy Saving

(MW)

Cold 9.903 0.46 9.443

Hot 36.695 27.22 9.475

Comparison Between Utilities Consumption Before And After Minimum Energy Recovery

In this plant, after the heat integration, the energy saving is concluded below.

Temperature – Interval Heat Balance

PROCESS FLOW SHEETING

PROCESS FLOW DIAGRAM (PFD)Before Heat Integration

After Heat Integration

PROCESS FLOW DIAGRAM (PFD)

METHANOL

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20

S1 S2 S3 S4 S5 S6 S7 S8 S9 S10 S11 S12 S13 S14 S15 S16 S17 S18 S19 S20

2026.54 2026.54 2026.54 2026.54 2026.54 2026.54 2026.54 5066.21 5066.21 5066.21 1519.84 1519.84 1519.84 1519.84 1519.84 241.42 2459 344.51 344.61 344.01

24.85 226.85 196.6 869.85 96.85 96.85 96.85 248.62 249.85 24.85 10.103 9.85 9.85 9.85 145.85 -172.57 178.01 102.76 98.991 125.88

330.00 990.00 1320.00 1882.366 1882.37 259.00 658.00 285.00 476.430 476.430 476.430 198.520 277.910 277.910 277.910 0.278 277.640 277.640 263.900 13.740

306.471 0 306.471 56.820 56.820 55.771 1.049 55.771 56.82 56.82 56.82 56.684 0.136 0.136 0.136 0.0001 0.135 0.135 0.135 0

13.464 0 13.464 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0

2.541 0 2.541 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0

0 990 990 585.510 585.510 55.771 1.049 55.771 13.609 13.609 13.609 0.108 13.502 13.509 13.509 0.0135 13.488 13.488 0.0135 13.475

0 0 0 169.953 169.953 1.45 0.0347 1.45 0.826 0.826 0.826 0.822 0.0038 0.0038 0.0038 0.000 0.004 0.004 0.004 0

6.039 0 6.039 120.288 120.288 25.635 559.875 25.635 6.014 6.014 6.014 5.954 0.060 0.060 0.060 0.000 0.060 0.060 0.060 0

0 0 0 948.310 948.310 119.085 1.203 119.085 118.109 118.109 118.109 117.827 0.282 0.282 0.282 0.000 0.282 0.282 0.282 0

0 0 0 0 0 0 0 0 275.729 275.729 275.729 12.879 262.850 262.850 262.850 0.263 262.587 262.587 262.587 0.263

1.485 0 1.485 1.485 1.485 1.485 1.485 1.485 1.485 1.485 1.485 1.481 0.0048 0.004 0.004 0.000 0.004 0.004 0.004 0

0 0 0 0 0 0 0 0 3.836 3.836 3.836 2.761 1.075 1.075 1.075 0.001 1.074 1.074 1.074 0

Stream (kmole/hr)

Pressure (kPa)

Temperature (°C)

METHANECOMPONENTS

Total flow rate (kmole/hr)

DIMETHYL ETHER

ETHANE

PROPANE

WATER

CARBON MONOXIDE

CARBON DIOXIDE

HYDROGEN

METHANOL

NITROGEN

Natural Gas to Methanol

ACETIC ACIDMethanol to Acetic Acid

21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44

S21 S22 S23 S24 S25 S26 S27 S28 S29 S30 S31 S32 S33 S34 S35 S36 S37 S38 S39 S40 S41 S42 S43 S44

101.3 101.3 101.3 2800 3000 150 150 231 101.3 300 236 101.3 101.3 101.3 101.3 101.3 101.3 101.3 101.3 101.3 101.3 101.3 101.3 101.3

40 40 27 188 181.9 108.4 108.4 86.9 100 400 139.5 40 65 95 90 77 80 65 95 90 77 30 77 27

75.729 78.869 117.066 69.000 278.490 271.850 6.649 13.077 13.557 16.550 245.242 114.887 21.772 3.786 135.911 99.940 158.366 53.957 53.957 53.957 46.910 17.986 46.910 140.380

75.729 78.869 0 0 3.853 0.4064 3.546 0.406 0 0.776 0 0 0 0 0 0 0 0 0 0 0 0 0 0

0 0 0 69.000 3.436 0.3325 3.103 0.333 0 3.436 0 0 0 0 0 0 0 0 0 0 0 0 0 0

0 0 117.066 0 123.325 123.235 0 12.338 6.169 12.338 104.756 85.740 3.786 3.786 81.954 81.954 0 0 0 0 0 0 0 0

0 0 0 0 147.875 147.875 0 0 7.388 0 140.486 0.222 0 0 35.971 0 140.38 35.971 35.971 35.971 35.971 0 35.971 140.38

0 0 0 0 0 0 0 0 0 0 0 28.925 17.986 0 17.986 17.986 17.986 17.986 17.986 17.986 10.939 17.986 10.939 0

CARBON MONOXIDE

WATER

ACETIC ACID

ETHYL ACETATE

Stream (kmole/hr)

Pressure (kPa)

Temperature (°C)

METHANOL

Total flow rate (kmole/hr)COMPONENTS

CONCLUSION

CONCLUSIONS

CONCLUSIONS

Process Background and Market

Survey

Feasibility Study and

Plant Location

Heat Exchanger NetworkCost and

Economic Potential

Optimization

Alternative Processes

Mass and Energy

Balances

RECOMMENDATIONS

RECOMMENDATIONS

A. HAZOP

B. Process Control

C. Waste Management

D. Mechanical Design

REFERENCES

REFERENCES

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New Jersey

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[11] Acetic Acid. Retrieved September 29, 2011 from the Wikipedia:

http://en.wikipedia.org/wiki/Acetic_acid

REFERENCES

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natural- gas-price-in-malaysia-still-cheaper-compare-with-neighbors.html

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Retrieved from http://www.greenpurchasingasia.com/content/eco-preneur-sees-abundance-amidst-waste

[15] Methanex ( 2011, September 30). Methanol Price.

Retrieved from http://www.methanex.com/products/methanolprice.html

[16] Lee H. (2011, August). Prices, market and analysis.

Retrieved from http://www.icis.com/V2/chemicals/9074786/acetic-acid/pricing.html

[17] Environmental Quality (Scheduled Wastes) Regulations, 1989, Environmental Quality Act 1974 (Act 127) &

Subsidary Legislation, ILBS, pg 168, 2003

[18] Kirk-Othmer (1975), ‘Encyclopedia of Chemical Technology’, Vol. 1

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