The document summarizes the design of a 30,000 MTPA maleic anhydride production plant in India. It includes:
1) An introduction describing the importance of maleic anhydride and the aim to design a cost-effective plant using mixed butane as a feedstock.
2) Details of the major process units - feedstock pretreatment, synthesis reactor, product recovery and purification.
3) Evaluation of four process alternatives and selection of the final design incorporating a catalytic partial oxidation reactor, absorber for product recovery, and distillation for purification.
4) Key aspects of the design such as mass balances, equipment sizing for a shell and tube heat exchanger, and the
To demonstrate the effect of cross sectional area on the heat rate.
To measure the temperature distribution for unsteady state conduction of heat through the uniform plane wall and the wall of the thick cylinder.
The experiment demonstrates heat conduction in radial conduction models It
allows us to obtain experimentally the coefficient of thermal conductivity of some unknown materials and in this way, to understand the factors and parameters that affect the rates of heat transfer.
To understand the use of the Fourier Rate Equation in determining the rate of heat flow for of energy through the wall of a cylinder (radial energy flow).
To use the equation to determine the constant of proportionality (the thermal conductivity, k) of the disk material.
To observe unsteady conduction of heat
To demonstrate the effect of cross sectional area on the heat rate.
To measure the temperature distribution for unsteady state conduction of heat through the uniform plane wall and the wall of the thick cylinder.
The experiment demonstrates heat conduction in radial conduction models It
allows us to obtain experimentally the coefficient of thermal conductivity of some unknown materials and in this way, to understand the factors and parameters that affect the rates of heat transfer.
To understand the use of the Fourier Rate Equation in determining the rate of heat flow for of energy through the wall of a cylinder (radial energy flow).
To use the equation to determine the constant of proportionality (the thermal conductivity, k) of the disk material.
To observe unsteady conduction of heat
Excess gibbs free energy models,MARGULES EQUATION
,REDLICH-KISTER EQUATION,VAN LAAR EQUATION
,WILSON AND “NRTL” EQUATION
,UNIversal QUAsi Chemical equation
Engineering Design—Definition; Types of Design in Thermo-Fluid Science; Difference between Design and Analysis; Classification of Design; General Steps in Design; Abridged Steps in the Design Process
Download Link (Copy URL):
https://sites.google.com/view/varunpratapsingh/teaching-engagements
Syllabus:
Availability and Irreversibility
Availability Function
Second Law Efficiencies
Work Potential Associated with Internal Energy
Waste Heat Recovery
Heat Losses – Quality vs. Quantity
Principle of Heat Recovery Units
Classification of WHRS on Temperature Range Bases
Commercial Viable Waste Heat Recovery Devices
Benefits of Waste Heat Recovery
Development of a Waste Heat Recovery System
Commercial Waste Heat Recovery Devices
West Heat Recovery Boiler (WHRB)
Recuperators- Regenerative, Ceramic, Regenerative Heat Exchanger
Thermal wheel/ Heat Wheel
Heat Pipe
Economiser
Feed Water
Heat Pump
Shell and Tube Heat Exchanger
Plate Heat Exchanger
Run-around coil
Direct Contact Heat Exchanger
Advantages and Limitations of WHRD’s
Presentation on Calculation of Polytropic and Isentropic Efficiency of natura...Waqas Manzoor
This presentation demonstrates comparison of calculation of Polytropic and Isentropic Efficiency of Natural Gas Compressor using Aspen HYSYS & using Manual Calculations. Complete derivation of equations of Polytropic and Isentropic efficiency, have also been demonstrated. The slight difference observed in the manually calculated values and Aspen HYSYS simulation, may be attributed to the calculation method of the software which is based on numerical integration.
Excess gibbs free energy models,MARGULES EQUATION
,REDLICH-KISTER EQUATION,VAN LAAR EQUATION
,WILSON AND “NRTL” EQUATION
,UNIversal QUAsi Chemical equation
Engineering Design—Definition; Types of Design in Thermo-Fluid Science; Difference between Design and Analysis; Classification of Design; General Steps in Design; Abridged Steps in the Design Process
Download Link (Copy URL):
https://sites.google.com/view/varunpratapsingh/teaching-engagements
Syllabus:
Availability and Irreversibility
Availability Function
Second Law Efficiencies
Work Potential Associated with Internal Energy
Waste Heat Recovery
Heat Losses – Quality vs. Quantity
Principle of Heat Recovery Units
Classification of WHRS on Temperature Range Bases
Commercial Viable Waste Heat Recovery Devices
Benefits of Waste Heat Recovery
Development of a Waste Heat Recovery System
Commercial Waste Heat Recovery Devices
West Heat Recovery Boiler (WHRB)
Recuperators- Regenerative, Ceramic, Regenerative Heat Exchanger
Thermal wheel/ Heat Wheel
Heat Pipe
Economiser
Feed Water
Heat Pump
Shell and Tube Heat Exchanger
Plate Heat Exchanger
Run-around coil
Direct Contact Heat Exchanger
Advantages and Limitations of WHRD’s
Presentation on Calculation of Polytropic and Isentropic Efficiency of natura...Waqas Manzoor
This presentation demonstrates comparison of calculation of Polytropic and Isentropic Efficiency of Natural Gas Compressor using Aspen HYSYS & using Manual Calculations. Complete derivation of equations of Polytropic and Isentropic efficiency, have also been demonstrated. The slight difference observed in the manually calculated values and Aspen HYSYS simulation, may be attributed to the calculation method of the software which is based on numerical integration.
Mono ethylene glycol is a chemical often used for plant and pipeline integrity management - but if used incorrectly it can have an adverse effect on a facility. Advisian’s Steve Cooper discusses what needs to be considered when working with MEG at the IChemE Hazards Australiasia Conference in Melbourne
Pilot Plant Scale Up Techniques Used in Pharmaceutical Manufacturing, Prof. Dr. Basavaraj K. Nanjwade, KLE University College of Pharmacy, Belgaum/Belagavi
The Selective Oxidation of n-Butane to Maleic Anhydride in a Catalyst Packed ...Gerard B. Hawkins
The Selective Oxidation of n-Butane to Maleic Anhydride in a Catalyst Packed Tubular Reactor
CONTENTS
0 INTRODUCTION
1 n-BUTANE OXIDATION
2 REACTION KINETICS
3 HEAT AND MASS TRANSFER PARAMETERS
4 NON-ISOTHERMAL, NON-ADIABATIC REACTOR MODELING
5 USE OF THE REACTOR MODEL IN OPERABILITY AND DESIGN STUDIES
6 BIBLIOGRAPHY
7 NOMENCLATURE
Heat transfer area and Heat transfer cofficient (U)abdullahkhalid50
Working on the radiator of Suzuki Baleno 1999.
How to calculate the overall heat transfer coefficient (U)?
How to calculate the heat transfer area and compare it with the experimental data being collected.
Heat/light/electrical energy is out today’s necessity and has scarcity also. Energy conservation is key requirement of any industry at all times.
In general, industries use heat energy for conservation of raw material to finished product. The source of heat energy is generally saturated or super heated steam. The steam generation is common use one boiler with carity of fuels. Whatever may be the fuel the generation should be as economy as possible which adds to the product cost. Further the usage of steam and recycling steam condensate back to boiler is an art depending on plant layouts.
In this project the steam generator is water tube boiler fired with rice husk. The steam is transferred to the tyre/tube moulds where tyres/tubes are cured while the heat is rejected to the tyres the condensate forms and this condensate is put back to the boiler. While doing so the steam is also stopped back to boiler without rejecting complete heat to the product. This gets flashed into atmosphere at feed water tank. The science of separation of condensate from steam saves energy. Better the separation more the fuel conservation.
In the steam generator the fuel is burnt to heat the water and form steam. This fuel burnt flue gas carries lot of energy, out through chimney. Prior to exhausting through the heat left in flue need to be recovered, through heat recovery mechanisms’. In this project an air-preheater condensate heat recovery unit is the major energy consuming station.
ECONOMIC INSULATION FOR INDUSTRIAL PIPINGVijay Sarathy
Thermal Insulation for Industrial Piping is a common method to reduce energy costs in production facilities while meeting process requirements. Insulation represents a capital expenditure & follows the law of diminishing returns. Hence the thermal effectiveness of insulation needs to be justified by an economic limit, beyond which insulation ceases to effectuate energy recovery. To determine the effectiveness of an applied insulation, the insulation cost is compared with the associated energy losses & by choosing the thickness that gives the lowest total cost, termed as ‘Economic Thickness’.
The following tutorial provides guidance to estimate the economic thickness for natural gas piping in winter conditions as an example case study.
ABSTRACT
Heat/light/electrical energy is out today’s necessity and has scarcity also. Energy conservation is key requirement of any industry at all times.
In general, industries use heat energy for conservation of raw material to finished product. The source of heat energy is generally saturated or super heated steam. The steam generation is common use one boiler with carity of fuels. Whatever may be the fuel the generation should be as economy as possible which adds to the product cost. Further the usage of steam and recycling steam condensate back to boiler is an art depending on plant layouts.
In this project the steam generator is water tube boiler fired with rice husk. The steam is transferred to the tyre/tube moulds where tyres/tubes are cured while the heat is rejected to the tyres the condensate forms and this condensate is put back to the boiler. While doing so the steam is also stopped back to boiler without rejecting complete heat to the product. This gets flashed into atmosphere at feed water tank. The science of separation of condensate from steam saves energy. Better the separation more the fuel conservation.
In the steam generator the fuel is burnt to heat the water and form steam. This fuel burnt flue gas carries lot of energy, out through chimney. Prior to exhausting through the heat left in flue need to be recovered, through heat recovery mechanisms’. In this project an air-preheater condensate heat recovery unit is the major energy consuming station.
1. CH-2451 PROJECT WORK
NARENDARAN.K (312211203031)
PRITHIVI RAJ.S (312211203040)
VIVEK KUMAR.R(312211203061)
SUPERVISED BY DR.M.SUBRAMANIAN
Department of Chemical Engineering
Sri Sivasubramaniya Nadar College of Engineering
Kalavakkam – 603 110, Kanchipuram (Dist)
Tamil Nadu, India
02-Jan-2015
DESIGN OF 30,000 MTPA MALEIC ANHYDRIDE PRODUCTION
PLANT
2. CONTENTS:
• Introduction
• Best process route
• Mass balance
• Equipment design
• Saftey
• Economic balance
• Conclusion
• References
02-Jan-2015 M Subramanian
3. INTRODUCTION:
3
Maleic anhydride (MAN) plays an important role in
over half of the global demand production of unsaturated polyester resins.
Thus, the aim of this project is to design a practicable plant which is cost-
effective, profitable and harmless to the environment. The project is to
design Maleic Anhydride production plant by using mixed butane as the
feedstock. The plant could be divided into four main processes which are
feedstock pretreatment, synthesis of MAN, recovery MAN and purification
of MAN
4. PROJECT BACKGROUND:
Uses of Maleic Anhydride:
• synthesis of unsaturated polyester resin
• plasticizers, surface coatings, agrochemicals, lubricants.
0%
10%
20%
30%
40%
50%
North American Japan Middle East Asia Europe/France/Italy
Percentage demand of Maleic Anhydride (2007-2011)
Market in Asia
INDIA: THIRUMALAI CHEMICALS LTD (60,000 TPA)
Thailand: PTT Group Company (15,000 TPA)
Indonesia: Chandra Asri Petrochemical (6000-7000 TPA)
8. Alternative 1: Converter + Condenser:
Mixed
butane
Air
Air
Isobutane
n-butane
Offgas
Offgas
Liquid MA
to solidify
Offgas
Lean solvent
MA rich
MA rich
10. Alternative 3: Converter +
Condenser:
Isobutane for sale
Mixed
butane
Air
n-butane
Offgas
Offgas
Liquid MA
to solidify
Lean solvent
11. Alternative 4: Converter +
Condenser:
Mixed
butane
Air
Isobutane for sale
n-butane
Offgas
Offgas
Liquid MA
to solidify
Offgas
Lean solvent
MA rich
MA rich
17. DESIGN OF COOLER(E-201):
Equipment Sizing:
Composition and Properties of Inlet and Outlet:
Stream
Tin (°C) Tout (°C) Tin (K) Tout (K)
Process fluid 256 120 529 393
Stream data of shell side
18. Stream data of tube side
Stream tin (°C) tout (°C) tin (K) tout (K)
Cooling water 30 40 303 313
Cooler duty=3435 kW
R (T1-T2)/(t2-t1)
R 13.6
S (t2-t1)/(T1-t1)
S 0.0442
Calculate correction factor, Ft
19. From the Figure 12.19: temperature correction factor. Retrieved from Chemical Engineering (Volume 6)
Coulson and Richardson
20. The value of Ft = 0.98
• Calculate mean temperature, ∆Tlm
∆Tlm can be calculated from the equation,
Then,
∆Tlm = 136.92 °C
• Calculate actual temperature difference
Ft∆Tlm = 134.19 °C
• Overall heat-transfer coefficient
Typical values of the overall heat-transfer coefficient for various types of heat exchanger are given in Table 12.1
in the Chemical Engineering (Volume 6) Coulson and Richardson book.
Assuming this is cooler
)(
)(
ln
)()(
12
21
1221
tT
tT
tTtT
Tlm
21. U = 300 W/m^2°C
Area of heat exchanger
Provisional area of heat exchanger, A can be obtained through the formula,
lmTUAQ
lmTU
Q
A
Then,
A = 85.33 m2
Tube Side
From Appendix A.5-2, Transport Processes and Unit
Material Carbon Steel
BWG number 18
Length of tube Lt (m) 2.5
Outer diameter, Dto (mm) 25.4
Inner diameter, Dti (mm) 22.1
Material Thermal Conductivity (W/m.K) 36
22. Heat transfer area of a tube, At:
At = 0.1995 m2
Number of tube, Nt:
𝑁𝑡 =
𝐴
𝐴 𝑡
𝑁𝑡 =
85.33
0.1995
𝑁𝑡 = 428 𝑡𝑢𝑏𝑒𝑠
Number of tubes per pass, Np
𝑁𝑡 =
428
2
𝑁𝑡 = 214 𝑡𝑢𝑏𝑒𝑠
Tube pitch is the distance between tube centre and formulated as
𝑃𝑡 = 1.25 × 𝐷𝑡𝑜
𝑃𝑡 = 1.25 × 25.4
𝑃𝑡 = 31.75 𝑚𝑚
For typical tube arrangements, from Table 12.4, Chemical Engineering (Volume 6) Coulson
and Richardson, for triangular pitch for 2 passes, the constant value as follows:
K1 = 0.249
n = 2.207
tott DLA
23. The bundle diameter, Db:
𝐷 𝑏 = 𝐷𝑡𝑜 𝑁𝑡 𝐾1
1 𝑛
𝐷 𝑏 = 25.4 428 0.249 1 2.207
𝐷 𝑏 = 0.743 𝑚
Shell internal Diameter, Ds
From Chemical Engineering (Volume 6) Coulson and Richardson, figure 12.10,
For Fixed and U-tube,
Shell-bundle clearance = 87 mm
= 0.087 m
Shell internal Diameter, Ds = Db + shell bundle clearance
Ds = 0.830 m
Tube side Coefficient
Mean temperature (K), Tm:
Tm = (Tcin +Tcout)/2
Tm = 308 K
Tube cross-sectional area, At:
𝐴 𝑡 =
𝜋𝐷𝑡𝑖
2
4
𝐴 𝑡 =
𝜋22.12
4
𝐴 𝑡 = 383.64 𝑚𝑚2
24. Total flow area (m2), AT:
𝐴 𝑇 = 𝑁𝑡. 𝐴𝑡
𝐴 𝑇 = 82098.96 𝑚𝑚2
= 0.821 𝑚2
𝐴 𝑇Physical properties of the tube side fluid are obtained from Appendix A.2-11, Transport
Processes and Unit Operation by, Christie J. Geankoplis:
Water density, ρt (kg/m3
) 996.2600
Viscosity of water, μtL (Ns/m2
) 8.348 x 10-4
Heat capacity, Cp (kJ/kg.K) 4.1798
Thermal conductivity, ktf (W/m.K) 0.6129
Table 1: Physical properties of water
25. Mass flowrate (inside tube), m= 81.27 kg/s
Fluid velocity, vf:
𝑣𝑓 = 𝑚 𝐴 𝑇
𝑣𝑓 = 81.27 0.821 = 98.99 𝑘𝑔 𝑚2
. 𝑠
Linear velocity, u
𝑢 = 𝑣𝑓 𝜌
𝑢 = 98.99 996.26 = 0.09937 𝑚/𝑠
Reynold number, Re
𝑅𝑒 =
𝜌𝑢𝐷𝑡𝑖
𝜇
=
(996.26)(0.09937(0.0221)
8.348 × 10−3
= 26210
Prandtl number, Pr
𝑃𝑟 =
𝜇𝐶 𝑝
𝑘 𝑓
=
(8.348 × 10−3
)(4179.8)
0.6129
= 5.693
Length of tube/Inner diameter (L/Dti) = 2.5/ 0.0221= 113.122
Heat transfer coefficient, jh= 0.0037
Tube side heat transfer coefficient, hi
ℎ𝑖 =
𝑘 𝑓 𝑗ℎ 𝑅𝑒𝑃𝑟0.33
𝐷𝑡𝑖
𝜇
𝜇 𝑤
0.14
= 4848.077 𝑊 𝑚2
K
We assume that viscosity of the fluid is identical at the wall and of the bulk fluid.
26. Tube Side Pressure Drop
Friction factor, jf = 0.0036
Tube side pressure drop can be calculated from the equation below:
Where,
m = 0.25 for laminar flow, Re<2100 ; m = 0.14 for turbulent flow, Re>2100
Np = number of tube side passes
ΔPt= 57.53 Pa
2
]5.2))(/(8[
2
sm
w
tifps
u
DLjNP
Shell Side
Fluid density, ρs (kg/m3
)
1.768
Viscosity, μsL (Ns/m2
)
2.073x10-5
Heat capacity, Csp (kJ/kg.K)
1.155
Thermal conductivity, ksf (W/m.K)
0.03081
Physical properties of reactor effluent
27. Shell Side Heat Transfer Coefficient
Shell diameter, Ds = 0.83 m
Tube pitch, Pt = 31.7500 mm = 0.0318 m
Cross flow area, As will be calculated using:
𝐴 𝑠 =
𝑝 𝑡−𝐷𝑡𝑜 𝐷 𝑠 𝑙 𝐵
𝑃𝑡
= 0.0689 m2
Shell side mass velocity, Gs :
𝐺𝑠 =
𝑤𝑠
𝐴 𝑠
=
77110
0.0689
= 310.88 𝑘𝑔 𝑠. 𝑚2
Shell side equivalent diameter, De
𝐷𝑒 =
1.1
𝐷𝑡𝑜
𝑝𝑡
2
− 0.971𝐷𝑡𝑜
2
= 16.526 𝑚𝑚
Mean temperature (K)
Tmean = (Th.in +Th,out)/2
Tmean = 461.0 K
mDlSpacingBuffle B 415.0*2/1,
mDDiameterBuffle s 8284.00016.0
28. Reynold number, Re
𝑅𝑒 =
𝐺𝑠 𝐷𝑒
𝜇
=
(310.88)(0.016526)
2.073 × 10−5
= 248383
Prandtl number, Pr
𝑃𝑟 =
𝜇𝐶𝑝
𝑘𝑓
=
(2.073 × 10−5
)(1.155)
0.03081
= 0.777
Selecting 25% for baffle cut
From figure 12.29, Chemical Engineering (Volume 6) Coulson and Richardson, the heat
transfer factor is:
Heat Transfer Factor, jh = 0.045
Shell side heat transfer coefficient, hs
hs= 19157.20 W/m2
.K
14.03/1
PrRe
we
hf
s
D
jk
h
29. Overall Heat Transfer Coefficient:
Outside fluid film coefficient, hs, W/m2
.o
C 3036139
Inside fluid film coefficient, hi, W/m2
.o
C 799.3244
Outside dirt coefficient (fouling factor), hod, W/m2
.o
C 6000
Inside dirt coefficient, hid, W/m2
.o
C (from Table 12.2, vol. Six ) 3000
Thermal conductivity of the tube wall material, kw, W/m.o
C 36
Tube inside diameter, Dti, m 0.0221
Tube outside diameter, Dto, m 0.0254
Overall heat transfer coefficient can be calculated by using the formula
So we get,
1/Uo = 0.002319
Uo = 492.153
Percentage difference = |(Ucal-Uass)/Uass|*100% = 64%
iti
to
idti
to
w
titoto
odso hd
d
hd
d
k
ddd
hhU
11
2
)/ln(111
30. Data/requisition sheet for
COOLER E-201
Equipment No.: E-201
OPERATING / MECHANICAL DATA
Type of heat exchanger Shell and Tube Heat Exchanger
Number of units required 1
Duty (W) 3435000
Heat transfer area (m2
) 85.33
Overall heat transfer coefficient
(W/m×°C)
492.153
Type of support Saddle
Insulation None
Parameters Shell Tube
Fluid Process Fluid Cooling Water
Material of construction Carbon steel Carbon Steel
Mass flow rate (kg/h) 77110 292600
Heat transfer coefficient (W/m2
.K) 19157.20 4848.07
Inlet temperature (operating) (°C) 256 30
Outlet temperature (operating) (°C) 120 40
Design temperature (°C) 200 35
Inlet pressure (operating) (kPa) 210 100
Design pressure (kPa) - 140
Bundle diameter (mm) - 743
Outer diameter (mm) 846.526 25.4
Inner diameter (mm) 830.0 22.1
Length (m) - 2.5
Number of tubes - 428
Tube per pass - 214
Total flow area (m2
) - 0.821
Pitch (mm) - 31.75 (triangular)
Baffle cut 0.25 -
Baffle spacing (mm) 415.0 -
Prepared
Checked
Approved
Date Eng, Process Rev By Appr. Date
Service Cool effluent from R-201
Equipment No. E-201
Project No.
32. SAFETY AND LOSS PREVENTION
HAZARD AND OPERABILITY STUDIES (HAZOP):
• HAZOP study is a formal procedure of hazard identification and
elimination procedures designed to identify the potential hazards,
safety issues and operability issues especially in process plant.
33.
34.
35.
36.
37.
38.
39. USD 15.7 mil / year
Invest USD 35.4 mil
Payback period 6 years, then
ROR 22%
ECONOMIC BALANCE(spreadsheet):
40. CONCLUSION:
• It has been proven conceptually that the establishment of new production
plant is feasible.
• The plant is to be operated in a continuous mode, which involves the
oxidation of n-butane to form maleic anhydride. The reactor selected for
this process is the fluidized bed reactor. The proposed plant design is
economically justified and is said to be viable for investment based on the
economic potential of the process.
. This project has been extremely helpful in cultivating and enhancing the
knowledge and skills at hand. As final year students ,the experience gained
through out the project has given the opportunity in designing a real
processing plant ,which has improved our understanding in the chemical
engineering field. Not only that ,other skills are also developed in the
process, which includes communication skills, management skills, and most
importantly, teamwork.
41. REFERENCES:
• ACGIH (1994)1994-1995 Threshold Limit Values for Chemical Substances and Physical Agents and Biological
Exposure Indices. American Conference of Governmental Industrial Hygienists, Cincinnati, OH.
• Bedford, T. (2003). Safety and Reliability: Proceedings of the Esrel 2003 Conference. Maastricht, the
Netherlands: Taylor & Francis.
• Bertola A., Ruggieri R. Process of Recovery of Maleic Anhydride from Reaction Gas Mixture, US Patent
5069687, December 1991.
• Chauvel A., Lefreve G. Petrochemical Process, Edition Technips, 1989.
• Contractor, R. M. (1999).DuPont’s CFB technology for maleic anhydride. Chemical Engineering Science, 54,
5627–5632.
• Cooley, S. D., & Powers, J. D. (1998).Maleic acid and anhydride. (John J. McKetta, Ed.)Encyclopedia of
chemical processing and design. Marcel Dekker, Inc.
• David M., Lafayette, Calif. Maleic Anhydride Recovery Method, US Patent 3818680, June 1974.
• Dr J. L. Burgess. (May, 1993). International Programme on Chemical Safety Poisons Information Monograph
63 Chemical. Retrieved from inchem.org:
http://www.inchem.org/documents/pims/chemical/pims063.htm#SectionTitle:2.1
• Dr M. Ruse. (October, 1997). International Programme on Chemical Safety Poisons Information Monograph
945 Chemical. Retrieved from inchem.org: http://www.inchem.org/document/pims/chemical/pims945.htm
• Fair, J. R., (1987) “Energy-Efficient Separation Process Design,” Recent Developments in Chemical Process
and Plant Design, Y.A. Liu, McGee, Jr., H.A. and Epperly, W.R. (eds.), John Wiley & Sons, New York.
42. • Jazayeri, B. (2003). Applications for Chemical Production and Processing.In W.-C. Yang
(Ed.), Handbook of Fluidization and Fluid-Particle Systems, Chemical Industries (pp. 421–
444). Marcel Dekker, Inc.
• Ralph L. Improvement in recovery o Maleic and Phthalic Acid Anhydrides, UK patent
GB763339, December 1956.
• Roy, S., Duduković, M. P., & Mills, P. L. (2000).A two-phase compartments model for the
selective oxidation of n-butane in a circulating fluidized bed reactor. Catalysis Today,
61(1–4), 73–85. doi:10.1016/S0920-5861(00)00352-7
• Suzanne S., Fouhy K., Stephen M. Seeking The Best Route for Maleic Anhydride, Chemical
Engineering, McGraw Hill, December 1993.
• Tandioy, O. M., Gil, I. D., & Sanchez, O. F. (2009).Modelling of maleic anhydride
production from a mixture of n-butane and butenes in fluidized bed reactor. Latin
American Applied Research, 39, 19–26.
• J. P. Plotkin, H. Coleman, PERP Pogramme, Maleic Anhydride, Nexant, Inc, US, 2009
• San J., World Maleic Anhydride Market to Reach 2.0 Million metric tons by 2012, CA,
PRWEB, US, 2008. Retrieved from http://www.newswiretoday.com/news/18766/
• Rapid Growth in World Demand for Maleic Anhydride, Our Chemical Information
Provider, US, 2010. Retrieved from http://www.newswiretoday.com/news/18766/
• R. Smith, Chemical Process Design and Integration, Capital Cost for New Design, Wiley, pg
17
43. • Max S. Peters, Klaus. D. Timmerhaus, Ronald E. West (2003), ‘Plant Design
and Economics for Chemical Engineers’, 5th Ed, Mc Graw. Hill
• R.K. Sinnott (2000), ‘Coulson & Richardson’s Chemical Engineering’, Volume
6, 3rd Ed., Butterworth Heinemann, Great Britain.
• William G. Sullivan, Elin M. Wicks, C. Patrick Koelling, ‘Engineering
Economy’, 14th Ed, Pearson International Edition
• Tchobanoglous, G. et. al., (1991). Wastewater Engineering: Treatment and
Reuse. Fourth Edition. Metcalf & Eddy Inc.
• Van Wegenen, H. D. (1984). Preliminary Survey Report: Occupational
Hazard Control Options for Chemical Process Unit Operations. NIOSH, Ohio,
101-20a.
• Dr M. Ruse. (October, 1997). International Programme on Chemical Safety
Poisons Information Monograph 945 Chemical. Retrieved from inchem.org:
http://www.inchem.org/document/pims/chemical/pims945.htm
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Poisons Information Monograph 63 Chemical. Retrieved from inchem.org:
http://www.inchem.org/documents/pims/chemical/pims063.htm#Section
Title:2.1
