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CHE 400 Thesis I & II
Suman Sarkar0802019
1
STUDY OF DIFFERENT TYPES OF ETP PROCESSES AND TO
DEVELOP A THEORETICAL COST EFFECTIVE MODEL OF
EFFLUENT TREATMENT PLANT (ETP) FOR TANNERIES OF
HAZARIBAGH
Supervisor
Dr. Easir Arafat Khan
Assistant Professor
Department of Chemical Engineering, BUET
2
Outline
• Background
• Objective
• Methodology (Experimental/ Simulation Principle-
Procedure)
• Results and Discussion
• Conclusion & Recommendation
3
Background:
4
In developing countries like Bangladesh water pollution
due to industrial wastewater is a serious concern. Most
of the industries in Bangladesh do not treat their
wastewater properly and let it go to the river which
cause the pollution of river water. These untreated
wastewater has very bad effect on agriculture, aquatic
plant, fish and human health.
Tanneries in Hazaribagh cause massive pollution to
Buriganga and nearby areas of Hazaribagh.
Objectives
5
To study the wastewater quality of several industries
and compare with national standards
To study installation & operating cost and efficiency of
different ETP
Compare the ETPs based on installation & operating
cost and efficiency and develop a theoretical cost
effective model of ETP for Tanneries of Hazaribag
Methodology
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Laboratory experiment (BOD, COD, DO, TDS, pH
measurement)
Industrial data analysis (cost analysis)
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Lab Experiment
BOD5 measurement:
Chemical procedure
BOD5 = DO5 – DO1
COD measurement:
Chemical procedure
Heating and instrumental measurement
Microsoft Office Word Document
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Lab Experiment cont’d
Direct instrumental measurement:
DO
TDS
pH
Lab Experiment cont’d
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Aeration(BOD5 )
HeatingCOD
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Lab Experiment cont’d
DO pH
TDS
Lab Experiment cont’d
Parameters
Chemicals
Industry Paint Industry DOE
Waste water
Treated water
Waste Water
Treated water
pH 3 7.3 6.93 7.03 6 - 9
BOD5 450 ppm 38 ppm 250 ppm 16 ppm 50 ppm
COD 1200 ppm 172 ppm 670 ppm 46 ppm 200 ppm
TDS 4288 ppm 1900 ppm 1130 ppm 870 ppm 2100 ppm
DO 0 5.35 ppm 0 6.1 4.5 - 8
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Parameter Tannery Effluent Department of Environment
(DOE)pH 3.88 6 - 9
BOD5(mg/l) 1454 50
COD(mg/l) 3386 200
TDS(mg/l) 14572 2100
DO(mg/l) 0.0 4.5 - 8
Cr(ppm) 987 0.5 (0.1 for Cr6+)
12
Lab Experiment cont’d
Industry of Chemicals
Paint Industry
No. of Employee 4 6
Working Shifts 1 3
Working Hours 8 24
Liquid effluent discharge (m3/d)
8 120
Point of discharge Unused open land Pond
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Industrial data analysis
Fixed Cost Annual variable cost
Chemicals Tk. 1300000 Tk. 800000
Paint Tk. 3050000 Tk. 6200000
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Cost analysis
Chemicals
Industry Paint Industry
Chemical Process
Biological Process
Chemical Process
Biological Process
Operating Cost
Tk. 121000
Tk. 78000 Tk. 3550000
Tk. 1252000
Installation Cost
Tk. 410000
Tk. 740000
Tk. 1150000
Tk. 1650000
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Cost analysis cont’d
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Cost analysis cont’d
Cost analysis cont’d
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Cost analysis cont’d
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Installation cost of Biological treatment process
units were larger than Chemical treatment process
units
Operation cost of chemical treatment process was
larger than biological treatment process
Cost analysis cont’d
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Cost analysis cont’d
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Paint Industry produces 10 times more effluent
than Chemicals Production Industry
The ratio of cost of
Material supply = 1.78:1
Consultancy-commissioning-supervision = 1.67:1
Civil work = 4.8:1
Total fixed cost = 2.346:1
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ETP Model
Presence of Cr
Cr neutralization methods
Adsorption
Sawdust
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ETP Model cont’d
Conclusion & Recommendation
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BOD, COD, TDS, DO, pH of treated water will
reach DOE specification
Cr removal will not reach DOE specification
Conclusion
24
Conclusion & Recommendation cont’d
Lab experiment
Low cost adsorbent having optimum pH 2.5 – 3.5
Presence of alkalinity, chloride, oil and grease,
phenol compounds, sulfide etc.
Sludge management
Recommendation
25
END of
Thesis I & II
CHE 408 Process Design Sessional I & II
Suman Sarkar0802019
26
Design of Natural Gas Processing with Hysis
simulation
Supervisor
Dr. Dil Afroza Begum
Professor
Department of Chemical Engineering, BUET
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Outline
• Objectives
• Project definition
• Available Process
• Design Basis
• Process Block Diagram
• Process Flow Diagram (PFD)
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Outline cont’d
• Comparison between raw & products gas
• List of Major Equipments
• Individual Major Equipment Design
• Mechanical Design
• P&I Diagram
• Overall Economic Analysis
30
Objectives
Ensuring more efficient and profitability Design
Improving plant control, operability
Reducing human error and time requirement
Eliminating process bottle necks and minimizing
process network
By hysis simulation:
Project definition:
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Project definition cont’d
• Location- Golapgonj, Sylhet
• Capacity-550 MMSCFD
• Raw materials-Raw Natural Gas From 3
Producing Gas Wells, DEAmine Solution, TEG.
• Utility- Cooling water, Electricity (2 MW Capacity),
Natural Gas.
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Available Process
• Gas Sweetening
Solid Bed Sweetening Process: Molucular Sieves
Aquasorption Process (Wash Water Process)
Selexol Process
Chemical Absorption Process(MEA,DEA,TEA
Processes)
The Holmes-Stretford Process
34
Available Process cont’d
• Gas Dehydration
Absorption Process(Methanol, Glycol Process)
Adsorption Process (Solid Dessicants, Alumina,
Silica Gel, Molecular Sieves)
Design Basis
35
Climate Condition:
Ambient Temperature-
Max- 35oC Min-12oC
Design max temp- 40oC Min temp-5oC
Annual Avg. Atmospheric pressure-0.11 MPa
Annual Avg. relative Humidity- 80%
Wind Velocity-52 miles/hr
Rain- Annual avg Rainfall- 2850 mm
Process Block Diagram
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PFD (Hysis Simulation):
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Comparison Between Raw Natural gas & Product gas
Raw Natural GasComponents CompositionMethane 0.8634
Ethane 0.0574
Propane 0.0088
i-Butane 0.0007
i-Butane 0.0005
n-Pentane 0.0005
n-Hexane 0.0003
H2O 0.0467
Nitrogen 0.0018
CO2 0.0204
Components Composition
Methane 0.930973
Ethane 0.053632
Propane 0.000658
i-Butane 0.000022
i-Butane 0.000014
n-Pentane 0.000007
n-Hexane 0.000002
H2O 0.000101
Nitrogen 0.002029
CO2 0.012562
Product Gas
List of Major Equipments
39
Equipment Name QuantityDesignation in the
HYSYS Simulation
Compressor 1 K-100
Heat Exchanger 2 E-100, E-102
Absorber 2 T-100, T-102
Separator 3 V-100, V-101, V-104
Pump 2 P-100, P-101
Storage Tank 1 V-106
Stripper Column 2 V-102, V-103
Stabilizer Column 1 V-105
40
Design Parameter
Separator Diameter: 8.12 ft
Minimum Separator height: 40.6
Thickness of the Separator: 3.3 ft
Microsoft Office Word Document
Gas-Liquid Separator
41
Design Parameter cont’d Microsoft Office Word Document
Pump (P-100) of Dehydration plant
Total frictional loss:
2.44 ft
Total head: 43.11 ft
Power requirement:
17.1hp
Material: cast iron
RPM: 1750
Flow capacity: 770GPM
(max)
Impeller size: 11-3/4”
Weight: 255 lbs
Price: $ 4662.00
Specification of pump:
Mechanical Design of Separator
42
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P & ID Diagram
Figure: P & I diagram for gas liquid separator
P & ID Diagram cont’d
44
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Overall Economic Analysis
Equipment Cost at Present(2014)- $1.088 million
Total Capital Investment - $ 6.12 million
Total Annual Expenses- $ 13.24 million
Net Profit After Tax(15%)- $ 15.4 million
Pay back period – 3 year 11 month
Salvage value- $ 0.532 million
Depreciation- $0.765 million/year
IRR i% = 24.58 %
ERR i% = 19.67%
Project life – 20 years
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THANK YOU
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