final year plant design i group fydp 8 production of methanol and acetic acid goh wai boon11120...
TRANSCRIPT
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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
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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
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INTRODUCTION
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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
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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.
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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.
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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
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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
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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
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LITERATURE REVIEW• Product Market Study
• Site Feasibility Study
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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
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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
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World Consumption for Methanol and Acetic Acid
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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
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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
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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
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SITE SURVEY
GEBENG INDUSTRIAL AREA,PAHANG
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KIDURONG INDUSTRIAL AREA,SARAWAK
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PAKA INDUSTRIAL AREA,TERENGGANU
RECOMMENDED AREA
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MAP OF PASIR GUDANG,JOHOR
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TELUK KALUNG INDUSTRIAL AREA,KEMAMAN,TERENGGANU
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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
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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
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PRELIMINARY HAZARD ANALYSIS
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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
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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
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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
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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
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CONCEPTUAL DESIGN
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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
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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
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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
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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
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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
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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.
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MASS BALANCE CALCULATIONS
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METHANOL
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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
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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
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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
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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
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ECONOMIC
POTENTIAL
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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
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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
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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:
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Thus, economic potential at level 2 is:
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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)
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The price of methanol for production over a period of 7920 operating hours is:
Thus, economic potential at level 2 is:
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Level 3 Economic Potential (EP3)
Natural Gas to Methanol
At Level 3, Economic Potential 3 is obtained from the following:
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Methanol to Acetic Acid
At Level 3, Economic Potential 3 is obtained from the following:
Level 3 Economic Potential (EP3)
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HEAT INTEGRATION
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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.
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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
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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
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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
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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
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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
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ACETIC ACIDAbove Pinch Design
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ACETIC ACIDBelow Pinch Design
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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
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PROCESS FLOW SHEETING
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PROCESS FLOW DIAGRAM (PFD)Before Heat Integration
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After Heat Integration
PROCESS FLOW DIAGRAM (PFD)
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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
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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
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CONCLUSION
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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
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RECOMMENDATIONS
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RECOMMENDATIONS
A. HAZOP
B. Process Control
C. Waste Management
D. Mechanical Design
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REFERENCES
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REFERENCES
[1] Geankoplis, Christie J., Transport Processes and Separation Process Principles, (2003), Pearson Education, Inc.
[2] Smith, R., (2005), Chemical Process Design and Integration, John Wiley &Sons, Ltd.
[3] William G.Sullivan , (2002), Engineering Economy, Twelfth Edition, Prentice-Hall
[4] Biegler L.T, Grossman I.E, Westerberg A.W (1997), ‘Systematic Methods of Chemical Process Design’, Prentice Hall Int.,
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[5] James M. Douglas (1988), ‘Conceptual Design of Chemical Processes’, International Edition, Mc Graw Hill Inc, New York
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[8] Methanol. Retrieved September 29, 2011 from the Wikipedia: http://en.wikipedia.org/wiki/Methanol
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[11] Acetic Acid. Retrieved September 29, 2011 from the Wikipedia:
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REFERENCES
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[14] Chen E. (2011, March). Eco-preneur sees abundance amidst waste.
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[17] Environmental Quality (Scheduled Wastes) Regulations, 1989, Environmental Quality Act 1974 (Act 127) &
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[18] Kirk-Othmer (1975), ‘Encyclopedia of Chemical Technology’, Vol. 1
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Q N A
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