Final Coursework

8/12/2019 Final Coursework

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Design of a Wastewater Treatment

Plant in Leeds, UKProfessor: Dr. C. Tizaoui

EG-M09/EGA327

Water and Wastewater Engineering

Group D:

Frederico Halfeld Clark Gomes, 744484Luiza Pessoa Moreira, 744482Luiza Nunes Rocha, 744499Pedro Henrique Guerra Alves, 744486Thales Said Orichio, 744488

College of EngineeringSwansea University

SwanseaWales, UK


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Contents

1. Introduction ..................................................................................................................... 4

2. Population ....................................................................................................................... 4

3. Flow rates Calculations ................................................................................................... 4

4. Domestic Wastewater ..................................................................................................... 5

4.1. Domestic Wastewater Characterization ...................................................................... 5

4.2. Designed Plant and Flow sheet ................................................................................... 6

4.2.1. Aerobic BioOxidation reactor ................................................................................. 8

4.2.1.1. Substrate (Dsticwaste) degradation...................................................................... 8

4.2.1.2. Nitrification .......................................................................................................... 8

4.2.1.3. Biomass decay ..................................................................................................... 8

4.2.2. Clarifier .................................................................................................................... 9

4.2.3. Granular media filter ............................................................................................... 9

4.2.4. Flow Splitting ........................................................................................................ 10

4.2.5. Belt Filter ............................................................................................................... 10

4.2.6. Sludge Drying ........................................................................................................ 10

4.2.7. Mixing unit ............................................................................................................ 11

5. Industrial Wastewater Treatment .................................................................................. 11

5.1. Industrial Wastewater Characterization .................................................................... 11

5.2. Designed Plant and Flow sheet ................................................................................. 12

5.2.1. Mixing Unit ........................................................................................................... 14

5.2.2. Aerobic BioOxidation reactors .............................................................................. 14

5.2.2.1. Glucose degradation........................................................................................... 14

5.2.2.2. Phenol degradation............................................................................................. 15

5.2.2.3. Biomass decay ................................................................................................... 15

5.2.3. Clarifier .................................................................................................................. 15

5.2.4. Granular media filter ............................................................................................. 15

5.2.5. Flow Splitting ........................................................................................................ 16

5.2.6. Belt Filter ............................................................................................................... 16

5.2.7. Sludge Drying ........................................................................................................ 16

6. Economic Evaluation .................................................................................................... 16

6.1. Domestic Wastewater Treatment Plant ..................................................................... 16

6.2. Industrial Wastewater Treatment Plant ..................................................................... 18

7. Environmental Impact Analysis .................................................................................... 20

7.1. Domestic WWT Plant Analysis ................................................................................ 20

7.2. Industrial WWT Plant Analysis ................................................................................ 207.3. Final Effluent Characteristics .................................................................................... 21


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8. Alternatives for Sludge Disposal .................................................................................. 22

9. Conclusion .................................................................................................................... 23

10. References ................................................................................................................. 23

Appendix AUnits Mass Balances and Streams Composition .......................................... 25

Appendix B

Meetings Minutes ......................................................................................... 35


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1. Introduction

This project aimed to design a new municipal wastewater treatment plant

using SuperPro Designer package for the city council of Leeds. The purpose of it isto replace the old WWT plant,which was not capable to achieve compliance withdischarge standards. The WWTP was designed to serve a current population of50,000 people and that after 50 years. The effluent to be treated is composed by adomestic wastewater stream and an industrial stream from a textile industry.

Leeds is a city situated in the West Riding, in the middle of the UnitedKingdom. It is a huge manufacturing centre for clothing, with many wool industries inparticular [1].

2. Population

It is known that population statistics are widely used to shape and planservices across the cities. Hence, understanding how the population is growing andchanging is critical for the effective planning of a Wastewater Treatment Plant.Analyses were made through the results of the Census conducted in Leeds andshowed that the population has increased by 5.1% from 2001 to 2011 [2]. This ratewas used in the calculation of population projections, thus considering that in everyten years the population would increase by 5,1%, in 50 years it would grow by(5,1%)5. The results are shown below:

Figure 1: Population Projections

By the end of 2063, the population would be 64119 but in order to make thecalculations easier, it was assumed a value of 65000 citizens for this year.

3. Flow rates Calculations

It is known that in the UK the current volume of water consumption is around

150 L/capita.day [3]. Using this value it was possible to calculate the flow rate, inlitters per day, defined by:

45000

50000

55000

60000

65000

70000

2013 2023 2033 2043 2053 2063

Population

Year

Population Projections


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(Equation 1)

WhereQ = flow rate (L/day);

V = volume (L/capita.day);P = population.

The value was obtained in L/day. In order to obtain the flow rate in litters perhour, it was divided by 24. So, the flow rate was found in litters per hour. With thisvalue and the concentration of each component of the wastewater it was possible tocalculate the flow rate of all of it.

(Equation 2)Where

Q= flow rate of each component(kg/h);

C = concentration of each component (kg/L);

In order to determinate the quantity of water present in the effluent, thedifference between the total flow rate and the sum of all components flow rateswould be the amount of water input.

All of these calculations were used for the design of both, the domestic andindustrial wastewater plant.

4. Domestic Wastewater

4.1.Domestic Wastewater Characterization

Initially, the flow rate found for domestic wastewater was 406250 L/h. Usingthis value and the Equation 2, the values below were found.

Table 1: Components Information

ComponentConcentration

(mg/L)Flow rate

(kg/h)

Dsticwaste 250 101.5625

A_VSS 70 28.4375I_VSS 35 14.21875

N_VSS 6.2 2.51875

NonBio_SS 78 31.6875

NonBio_TDS 250 101.5625

NO2_NO3 2.5 1.015625

Ammonia 19 7.71875

Carbon dioxide 30 12.1875


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The flow rate of the water was obtained as described before and it was foundto be 388103 kg/L. At this point, it was necessary to characterize each constituent foruse the SuperPro Designer software. All the componentsproperties were providedin the coursework paper task.

Table 2: Components Environmental Properties

Property\Component Dsticwaste A_VSS

biomass

I_VSS

biomass

N_VSS

biomass

NonBio_SS NonBio_TDS NO2_NO3

COD (g O2/g) 1.80 1.36 1.45 1.38 0.00 0.00 0.00

ThOD (g O2/g) 1.80 1.36 1.45 1.38 0.00 0.00 0.00

BODu/COD (g/g) 1.00 0.85 0.83 0.80 0.00 0.00 0.00

BOD5/BODu (g/g) 0.68 0.68 0.68 0.68 0.00 0.00 0.00

TOC (g C /g) 0.60 0.50 0.50 0.50 0.00 0.00 0.00

TP (g P /g) 0.00 0.05 0.05 0.05 0.00 0.00 0.00

TKN (g N /g) 0.07 0.12 0.12 0.12 0.00 0.00 0.00

NH3-N (g N /g) 0.00 0.00 0.00 0.00 0.00 0.00 0.00

NO3-N (g N /g) 0.00 0.00 0.00 0.00 0.00 0.00 0.23

Kmaxo(mg substr/gbiomass.h)

76 0.00 0.00 0.00 0.00 0.00 0.00

Ks (mg/L) 0.4170 0.00 0.00 0.00 0.00 0.00 0.00

CaCO3 (g/g) 0.00 0.00 0.00 0.00 0.00 0.00 0.00

TS (g solids/g) 0.00 1.00 1.00 1.00 1.00 1.00 1.00

TSS/TS (g/g) 0.00 1.00 1.00 1.00 1.00 0.00 0.00

VSS/TSS (g/g) 0.00 0.90 0.90 0.90 0.00 0.00 0.00

DVSS/VSS (g/g) 0.00 0.80 0.80 0.80 0.00 0.00 0.00

VDS/TDS (g/g) 0.00 0.00 0.00 0.00 0.00 0.00 0.00

DVDS/VDS (g/g) 0.00 0.00 0.00 0.00 0.00 0.00 0.00

In the interest of achieving the UK wastewater discharge standards thefollowing unit operations were chosen to constitute the process.

4.2.Designed Plant and Flow sheet

The flow sheet of the domestic wastewater treatment plant is presented in.The unitsspecifications, dimensions and input and output streams are described inthe sub items as follow.


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Figure 2 : Domestic WWT Plant Flowsheet


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4.2.1.Aerobic BioOxidation reactor

It was needed to operate with two aeration biooxidation reactors in parallel.These bioreactors were used in order to digest the domestic waste, transforming theorganic matter and other compounds in a well-mixed basin under aerobic conditions.

In favour of the use of this process its necessary to define the reactions that willoccur in the reactor. Besides that, the kinetic constant and the stoichiometry also hadto be predetermined. The reactions are described below.

4.2.1.1. Substrate (Dsticwaste) degradation

gggggg

COOHVSSAONHDsticwaste

9.0

2

8.0

2

8.04.1

2

1.0

3

1

_

k = 2.4 mg BOD5/(mg vss.d). The above rate constant is assumed to apply for T =

20

o

C. The impact of temperature variations is accounted for by assuming a thetavalue of 1.08.

Ks = 8.1 mg BOD5/L

It was necessary to convert the kinetic constants from milligrams of BOD5 perlitter to milligrams of domestic waste (Dsticwaste) per litter. To accomplish this stepthe information in Table 2 were used.

4.2.1.2. Nitrification

gggggg

NONOOHVSSNCOONH2.257.7

2

0.18.1

2

6.24

2

5.7

3_2_3

k = 0.95 mg NH3-N/(mg N_VSS.d)

The above rate constant is assumed to apply for T = 20 oC. The impact oftemperature variations is accounted for by assuming a theta value of 1.023.

Ks = 1.5 mg NH3/L

4.2.1.3. Biomass decay

Reaction 1:

ggggggg

CONHOHSSNonBioVSSIOVSSA

45.1

2

1.035.0

2

1.02.015.1

2

05.1

3___

Reaction 2:

ggggggg

CONHOHSSNonBioVSSIOVSSN

45.1

2

1.035.0

2

1.02.015.1

2

05.1

3___

kd = 0.00325 1/h


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The above rate constant is assumed to apply for T = 20 oC. The impact oftemperature variations is accounted by assuming a theta value of 1.089.

Both reactors have the same dimensions. The tank depth was 3.50 m, thelength of the tank was 56.07, and width was 22.43 m. The Hydraulic Residence Timeof determined as 18 h, and the dissolved oxygen was 2 mg/L, for one and the other.

On the first reactor there are four streams the S-126 is the one that feedsthe reactor. The S-108 is the input of air into the unit process. Those are the inputstreams. The output streams are the S-104, which is the nitrogen emission stream,and the S-127 that is the stream that carries on the effluent further to complete thetreatment (main branch). The second reactor follows the same standard of the firstone. Although the feed input is the S-125, the air input is the S-119. The nitrogenemission output is the S-124 and the last one is the S-128.In both reactors all thereactions above happened with the extend achieved present in the table below:

Table 3: Reactions efficiency

Reaction Extend Achieved

Biomass Decay 1 100%

Biomass Decay 2 7%

Nitrification 100%

DsticwasteDegradation

100%

4.2.2.Clarifier

This unit operation was used to remove solid particulates from liquids. The

outputs are clarified water and sludge. It was use two clarifier, one before the aerobicBioOxidation reactor and another after the reactor. The first one has the followingdimensions, a surface area of 306.24 m2, a tank depth of 3.00 m, the tank diameteris 19.75, and a volume of 918,711.48 L. This clarifier removed 10% of A_VSSbiomass, I_VSS biomass, N_VSS biomass and had a removal efficiency of 70% ofNonBio SS. The particles in sludge were 10 g/L. The stream Input feed this unitand there are three output streams accomplishing it. The stream S-102 is theoutput for emissions but for this unit none of the components were chosen to beemitted. The S-101 is the main line and the S-106is the sludge stream.

Beyond the point of the second clarifier the influent was divided in two parts,one was directed to recycling while the other was sent to a granular media filter. Thesurface area of the second clarifier is 372 m2, the tank depth is 3.00 m and the tankdiameter is 21.79m. The volume of tank is 1,118,984.57 L. The A_VSS biomass,I_VSS biomass, N_VSS biomass and NonBio SS had 90% of removal efficiency.Additionally, the particles in sludge were 10 g/L. The input of this unit is the streamS-103 and the outputs are the S-110 which represents an emission that followsthe same as S-102, the S-112 that is the main line and the Sludge stream.

4.2.3. Granular media filter

Granular media filter removes additional suspended solids and oils. It is also a

polishing step that lowers the levels of suspended solids and associatedcontaminants in treated wastes. The removal of particles takes place either on the


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surface of the media (cake filtration) or throughout the depth of the media (depthfiltration). In the granular media filtration process, particles typically adsorb or attachto the grains of sand or anthracite in the filter [4].The bed depth is 2.13 m and thebed diameter is 1.50 m. As the volume that we are working with is huge, it would beneeded six units of granular media filters with the dimensions mentioned above. The

A_VSS biomass, N_VSS biomass and NonBio SS had 90% of removaleffectiveness. There are two input streams which are the S-112 carrying the feedand the S-116 that adds water to the process. The S-105 is the backwash flowthat contains A_VSS biomass, N_VSS biomass and NonBio SS, and the otherstream is the output of the domestic WWTP.

4.2.4.Flow Splitting

A procedure was used to split two bulk flow streams. It was used two flowssplitting. The first one was used to split the stream S-115, which comes out of thefirst clarifier, into the streams S-125 and the S-126. Those two streams are theones who feed both reactors. The S-115 was split in half. The second flow splittingwas used to separate the sludge stream that comes out of the second clarifier intothe S-114 and the sludge recycle stream. The flow was split in 25% to the topstream and the remaining to the down stream. The top stream, which is the sludgerecycle one, feed a mixer that sends this flow to the aerobic biooxidation reactor. TheS-114 stream was also linked to a mixer that later on would feed the Belt filtrationprocess.

4.2.5.Belt Filter

A Belt Filter Press is a sludge dewatering device that applies mechanicalpressure to a chemically conditioned slurry, which is sandwiched between twotensioned belts, by passing it through a serpentine of decreasing diameter rolls. Thematerial balances are based on the removal percentage of particulate componentsand the solids content of the cake. The belt width is 0.49 m. The A_VSS biomass,I_VSS biomass, N_VSS biomass and NonBio SS had 90% of removal efficiency.The specific sludge rate was 300 (kg/h)/m and the solids recovery were 90%. Also,the solids presents in the cake were 15 wt/wt cake. The sludge treatment line is thefeed stream of influent and the S-111 is the input of water.There are two outputstreams: the S-113 which takes the filtrate to the biooxidation reactor and the S-120 which carries the sludge to the sludge drying.

4.2.6.Sludge Drying

Sludge drying procedures are based on contact, convection or radiationprocesses. Large amounts of air are not necessary during the contact drying,because the warmth is supplied by the contact between the damp product and aheated wall. Only a minimum gas flow is often planned for the evacuation of steam[5].The evaporative capacity of the sludge drying is 531.92kg/h. The solids presentin dried sludge were 35%. The input of sludge is the S-120, while the S-121is theair input. The S-122 is the output for nitrogen, I_VSS biomass and oxygen whilst

the other output stream is the dried sludge.


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4.2.7.Mixing unit

The mixing unit precedes the biological treatment aiming to mix the fourstreams, which constitute the total stream entering the biological treatment units. Themixing unit mixes the wastewater from the domestic process itself, the sludge

recycling stream, the waste stream from the Belt Filtration unit and the waste streamfrom the Granular Medium Filtration unit. The waste streams are added in intentionto reduce the liquid waste from the WWT plant. The second mixing unit was usedbefore the clarifier with the purposes to gather the streams, S-127 and S-128,which were getting out of both aerobic biooxidation reactor. The third mixer precededthe belt filtration with the intention to converge the streams S-106 and S-114 intothe sludge treatment line.

5. Industrial Wastewater Treatment

5.1.Industrial Wastewater Characterization

The industrial wastewater comes from a textile industry and thecharacteristics of the stream were determined with data from the literature, which willbe presented ahead.

The flow rate found for the sewage of a textile industry that processes 1000meters of textile fabric was 342700 L/h [6]. The characteristics of the industrialinfluent are given on Table 4.

Table 4: Components information

ComponentConcentration

(mg/L)Flow rate

(kg/h)

Glucose 806 276.216

NO2_NO3 2.4 0.822

Ammonia 1.18 0.404

Phenol 0.285 0.098

Carbondioxide

376 128.855

Heavy Metals 12.91 4.424

The COD and alkalinity data were taken from the average on the six textileindustries analysed by Paul et al. (2013). The COD average is 859.2 mg/L. Hence,considering that 1g of glucose gives 1.066 g of COD, we could find the concentrationof glucose in the stream. The alkalinity average is 376 mg/L, which representscarbon dioxide in its dissolved forms.

The value of 0.285 mg/L was selected for phenol as an average of the datafrom the mixed points of the textile effluent according to Nosheen et al. (2000).

From Khan et al. (2006) we have the parameters for nitrate and ammonia asan average of the wastewater parameters for different industries. The component

Heavy Metals was determined as a sum of concentration of the metals (Cd, Cr, Cu,


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Fe, N, Mn and Zn) analysed by Imtiazuddin et al. (2012). The contribution of eachmetal is presented in Table 5.

Table 5: Heavy Metals Concentration

MetalsAverage

Composition (mg/L)

Cd 0.07

Cr 1.39

Cu 2.72

Fe 1.96

Ni 0.99

Mn 1.27

Zn 4.51

Total Heavy

Metals12.91

5.2.Designed Plant and Flow sheet

The flow sheet of the industrial wastewater treatment plant is presented in.The units specifications, dimensions and input and output streams are described inthe sub items as follow.


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Figure 3: Industrial WWT Plant flowsheet


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5.2.1.Mixing Unit

The mixing unit has the same function as described in 3.1 but it mixes otherfour streams, the input, the sludge recycling, S-117and S-105. The S-117 streamis the backwash flow from the granular medium filter and the S-105 stream is the

waste flow from the belt filter. The output stream of this unit is the S-102 stream.

5.2.2.Aerobic BioOxidation reactors

The bioreactors were used in order to digest the organic content of theindustrial waste under aerobic conditions and to remove heavy metals by sorption tothe biomass produced, which will be removed in the clarifier. The reactions occurringin this unit and their kinetic constants and stoichiometry are described below insections 4.2.2.1 to 4.2.2.3.

Two aerobic bio oxidation reactors in series were required to produce water in

accordance to United Kingdom standards for wastewater discharge.Both aeration basins have a total volume of 2,099,980.92 litres. The reactorshave a rectangular configuration, with length of 38.73 m and width of 15.49 m, anddepth of 3.5 meters. The hydraulic detention time is 6 hours, with a dissolved oxygenconcentration of 2 g/L. The reactors work with a surface aeration system. For thedesign, 90 % of the heavy metals are removed by sorption to the biomass.

The first aeration tank receives the S-102 stream and an air stream to supplyoxygen for the aerobic reactions (S-113). This reactor emission is represented as theS-103 stream, which is composed of carbon dioxide. The S-104 stream continues totreatment entering the second reactor.

The second reactor also has an input air stream (S-120) to provide oxygen.

The gas emission of this reactor is also composed of carbon dioxide and isrepresented by S-108 stream. The output stream of the reactor (S-106) goes to theclarifier to solids sedimentation.

The extend achieved for each reactions is presented in table 6.

Table 6: Reactions extend achieved

Reaction Aeration Basin 1 Aeration Basin 2Glucose

Degradation86.193% 100%

PhenolDegradation

99.057% 0.00%

Biomass decay 59.702% 19.870%

5.2.2.1. Glucose degradation

gggg

COOHVSSAeGlu

3.0

2

3.0

2

4.01

_cos

k = 0.08 1/h. The above rate constant is assumed to apply for T = 20 oC. The impactof temperature variations is accounted by assuming a theta value of 1.04.

Ks = 5 mg glucose/L.


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5.2.2.2. Phenol degradation

gggg

COOHVSSAPhenol

3.0

2

4.0

2

3.00.1

_

k = 0.097 1/h.


Ks = 7.462 mg Phenol/L

5.2.2.3. Biomass decay

ggggggg

CONHOHSSNonBioVSSIOVSSA45.1

2

1.035.0

2

1.02.015.1

2

05.1

3___

kd = 0.00325416 1/h.


5.2.3.Clarifier

The Clarifier in question was set with a surface area of 355.80 m2, withdiameter of 21.28 meters, and a depth of 3m, resulting in a total volume of1,218,035.15 L. In this equipment 90% of the A_VSS and 90% of NonBio SS wereremoved.

The clarifier receives the S-106 stream from the second aeration tank. Noemissions were considered in this unit. The output streams are the S-121 thatcontinues to the treatment entering the granular media filter, and the sludge stream.The sludge stream is lead to the flow splitting unit.

5.2.4.Granular media filter

Generally used after gravity separation, Granular Media is a polishing stepthat lowers the levels of suspended solids and associated contaminants in treatedwastes. Particle removal takes place either on the surface of the media (cakefiltration) or throughout the depth of the media (depth filtration).

It was used a base unit with a bed depth of 2.02 m and a bed diameter of 1.5m. In order to achieve the total volume of wastewater that needs to be treated, 10granular media filters were used in this step. The overall removal efficiency was90%.

The S-121 stream from the clarifier is filtered and the main product of this unit,and also of the whole process, is represented by Output stream. The S-119 streamrepresents the backwash water input and the S-117 is the waste from this process,which is orientated to the mixing unit at the beginning of the plant.


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5.2.5.Flow Splitting

The flow splitting unit of the plant splits the sludge stream that comes from theclarifier in two streams: 25% of the sludge stream is recycled to the first aeration tankand the left amount goes to the sludge treatment line, entering the Belt Filtration unit.

5.2.6.Belt Filter

A belt filter was selected to provide increase in solids concentration of thesludge with a low area requirement. The belt width is 0.34 m. The belt filter workswith 90% of sludge recovery and 15% of solids in cake. The unit works with 90% ofremoval of A_VSS biomass, I_VSS biomass and NonBio SS.

The unit receives the sludge treatment line and a water stream (S-112). TheS-105 stream is the waste stream of the unit process and is redirected to the mixingunit. The S-111 stream goes to the sludge drier with a higher solids concentration

then before.

5.2.7.Sludge Drying

The sludge drying process consists in a reduction of moisture throughevaporation of water, using energy to reach the evaporation rate desired.

In this case, the evaporative capacity used was 337.86 kg/h, reaching 35% ofsolids in dried sludge.

The S-111 stream enters the unit and is concentrated, resulting in the driedsludge stream. The S-114 stream is the air to the process and the S-116 stream iscomposed of the air and water evaporated in the process.

6. Economic Evaluation

6.1.Domestic Wastewater Treatment Plant

Analysing the data given and, adding to it, the knowledge obtained throughresearch, the simulations were performed in SuperPro Designer and an EconomicReport was generated.

In an executive summary, the Total Capital Investment obtained was101,178,000 $, with an Operating Cost of in 21,020,00 $/yr.

As part of an initial investment analysis, the Costs of Units were taken into

account and the results obtained are shown as in Table 7.Table 7: Equipment Costs

Quantity Name Unit Cost ($) Total Cost ($)

1 Aeration Basin [1] 4,944,000 4,944,000

1 Clarifier [1] 333,000 333,000

6 Granular Media Filter 500,000 3,000,000

1 Belt Filter 244,000 244,000

1 Sludge Dryer 31,000 31,000

1 Clarifier [2] 296,000 296,000

1 Aeration Basin [2] 4,944,000 4,944,000


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The sum of all costs with the units results in a total cost of 13,792,000 $ forthe plant.

Along the Economic Evaluation a Fixed Capital Estimate Summary is made,based on the data of the software used, resulting in Table 8:

Table 8: Fixed capital estimate summary

Total Plant Direct Cost (TPDC)(physical cost)

Equipment Purchase Cost 17,240,000

Installation 2,587,000

Process Piping 6,034,000

Instrumentation 6,896,000

Insulation 517,000

Electrical 1,724,000

Buildings 7,758,000

Yard Improvement 2,586,000

Auxiliary Facilities 6,896,000

TPDC 52,239,000

Total Plant Indirect Cost (TPIC)

Engineering 13,060,000

Construction 18,283,000

TPIC 31,343,000

Total Plant Cost (TPC = TPDC+TPIC)TPC 83,582,000

Contractor's Fee & Contingency(CFC)

Contractor's Fee 4,179,000

Contingency 8,358,000

CFC 12,537,000

Direct Fixed Capital Cost (DFC =TPC+CFC)

DFC96,119,000

As a following step, the Labor Cost Analysis was made based on the selectedlabour type, such as Dryer Operator, and the rates of Unit Cost ($/h) combined withthe total of hours of usage. These calculations resulted in a total annual cost of2,709,275 $, with an annual amount of hours of 38,469 h.

Similarly to the Labor Cost Analysis, an Utilities Cost Evaluation is madetaking into account Std Power and Steam and its Unit Costs combined with theAnnual Amount, resulting in a total cost of 50,668 $.

As a final step in the Economic Evaluation, an Annual Operating Cost is made

compiling all the costs in the plant. Summing the costs from the plant, a Total AnnualOperating Cost obtained is equal to 21,020,000 $.


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6.2.Industrial Wastewater Treatment Plant

Following the same steps as did with the Domestic Wastewater, an EconomicEvaluation of the Industrial Wastewater Plant is performed using the data from thesimulations in SuperPro Designer.

The Executive Summary generated for this plant gives a Total InvestmentCost of 86,041,000 $. Besides that, an Operating Cost rate is calculated, resulting in18,158,000 $/yr.

As did before in the previous Economic Evaluation, the equipment costs wereused to give an overall cost for the major units. The results can be seen as in Table9:

Table 9: Equipment Costs

Quantity Name Unit Cost ($) Total Cost ($)

1 Clarifier 324,000 324,000

10

Granular Media

Filter 485,000 4,850,000

1 Belt Filter 244,000 244,000

1 Sludge Dryer 31,000 31,000

1 Aeration Basin [1] 3,079,000 3,079,000

1 Aeration Basin [2] 3,079,000 3,079,000

The sum of the costs of all units results in a total equipment value of11,607,000 $.

As a part of consummating the evaluation, a fixed capital summary is madeand the values obtained are shown as in Table 10:


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Table 10: Fixed capital estimate summary

Total Plant Direct Cost (TPDC)(physical cost)

Equipment Purchase Cost 14,509,000

Installation 2,623,000

Process Piping 5,078,000

Instrumentation 5,804,000

Insulation 435,000

Electrical 1,451,000

Buildings 6,529,000

Yard Improvement 2,176,000

Auxiliary Facilities 5,804,000

TPDC 44,408,000

Total Plant Indirect Cost (TPIC)

Engineering 11,102,000

Construction 15,543,000

TPIC 26,645,000

Total Plant Cost (TPC = TPDC+TPIC)

TPC 71,053,000

Contractor's Fee & Contingency(CFC)

Contractor's Fee3,553,000

Contingency 7,105,000

CFC 10,658,000

Direct Fixed Capital Cost (DFC =TPC+CFC)

DFC 81,711,000

Moving forward in the process of doing an Economic Evaluation, a Labor CostSummary is made using the same labor types as did before and the results obtained

culminated in a Total Annual Cost of 2,631,206 $, with an annual amount of hours of37,337h.Following the same steps as in the previous evaluation, the Utilities Cost

Evaluation uses again the Std Power and the Steam to obtain a total cost of 50,668$.

Finally, in order to accomplish a complete Economic Evaluation, a TotalAnnual Operating Cost is obtained, resulting in 18,158,000 $.


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7. Environmental Impact Analysis

7.1.Domestic WWT Plant Analysis

The environmental properties of the input and output of the domesticwastewater treatment plant and the removal efficiency of the parameters are shownin Table 11.

Table 11: Environmental Parameters

ParameterDomesticInput (kg/h)

DomesticOutput (kg/h)

RemovalEfficiency

TOC (mgC/l) 204.56 10.334 95%

COD (mgO/l) 601.447 29.151 95%

ThOD (mgO/l) 601.447 29.151 95%

BODu (mgO/l) 576.953 24.591 96%

BOD5 (mgO/l) 392.328 16.722 96%

TKN (mgN/l) 30.688 2.44 92%

NH3 (mgN/l) 0 0 0

NO3/NO2 (mgN/l) 0.572 8.086 -1314%

TP (mgP/l) 5.532 1.001 82%

TS (mgSlds/l) 439.465 279.997 36%

TSS (mgSlds/l) 188.243 21.311 89%

VSS (mgSlds/l) 99.574 18.019 82%

DVSS (mgSlds/l) 79.659 14.415 82%

TDS (mgSlds/l) 251.222 258.686 -3%

VDS (mgSlds/l) 0 0 0

DVDS (mgSlds/l) 0 0 0

It can be seen in the table above that the domestic wastewater plant had asatisfying removal efficiency of COD and BOD5 as expected, once that the highorganic matter removal is a characteristic of the activated sludge process. Although,the removal efficiency of NO3/NO2 was negative but this was expected once that

these components are formed in the nitrification reaction (3.1.2.). Besides, the TDSrate was negative, which can be related to the increase of NO3/NO2.

7.2.Industrial WWT Plant Analysis

The environmental properties of the input and output of the domesticwastewater treatment plant and the removal efficiency of the parameters are shownin Table 12.


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Table 12: Environmental Parameters

ParameterIndustrial Input(kg/h)

Industrial Output(kg/h)

RemovalEfficiency

TOC (mgC/l) 321.3 8.391 97%

COD (mgO/l) 856.36 23.456 97%ThOD (mgO/l) 856.07 23.276 97%

BODu (mgO/l) 626.361 19.393 97%

BOD5 (mgO/l) 563.725 13.188 98%

TKN (mgN/l) 0 1.981 -100%

NH3 (mgN/l) 0 0 0

NO3/NO2 (mgN/l) 0.55 0.436 21%

TP (mgP/l) 0 0.826 -100%

TS (mgSlds/l) 805.096 18.609 98%

TSS (mgSlds/l) 0 16.712 -100%

VSS (mgSlds/l) 0 14.86 -100%

DVSS (mgSlds/l) 0 11.888 -100%

TDS (mgSlds/l) 805.096 1.897 100%

VDS (mgSlds/l) 802.706 0 100%

DVDS (mgSlds/l) 802.706 0 100%

As observed, the plant had shown high removal rates of organic matter asexpected and these values were slightly higher than the domestic WWT plant since

the activator sludge reactors were set in series. The values obtained for TKN, TP,TSS, VSS and DVSS were -100% due to the fact that these parameters were onlyproduced during the process.

7.3.Final Effluent Characteristics

The output of both plants is going to be mixed before discharge in theenvironment. The final effluent characteristics are defined in Table 13.


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Table 13: Final Effluent Environmental Parameters

ParameterFinal Effluent(kg/h)

TOC (mgC/l) 9.381

COD (mgO/l) 26.358

ThOD (mgO/l) 26.269

BODu (mgO/l) 22.042

BOD5 (mgO/l) 14.989

TKN (mgN/l) 2.215

NH3 (mgN/l) 0.000

NO3/NO2 (mgN/l) 4.334

TP (mgP/l) 0.915

TS (mgSlds/l) 151.794

TSS (mgSlds/l) 19.055

VSS (mgSlds/l) 16.470

DVSS (mgSlds/l) 13.176

TDS (mgSlds/l) 132.739

VDS (mgSlds/l) 0.000

DVDS (mgSlds/l) 0.000

The final effluent is in accordance to the United Kingdom standards forwastewater discharge, which are 20mg/L of BOD5 and 30mg/L of TSS. Additionally,the nutrients concentrations also met the standards for sensitive areas (P: 1-2 mg/Land N: 10-15 mg/L) [11, 12].

8. Alternatives for Sludge Disposal

After passing through the Dryer, the sludge in the end of the process couldhave different destinations, such as Landfill, Composting Plant or even Blending.

In case the option chosen as final destination is landfill, the sludge would betransported in special trucks to the landfills and in there the sludge would becorrectly disposed in areas with the proper equipment to receive and storage it.

As a second option, the sludge could be transported from the WastewaterPlant to a Composting Plant. Once it reaches the destination, the sludge would beproperly treated and its nutrient levels would be enhanced in order to be used indifferent agricultural areas, such as farms and plantations, working as a fertilizer.

One new alternative that is becoming more frequent in many differentcountries is the process of blending the sludge. This process involves mixingindustrial waste including sludge - with diverse physical characteristics, turningthem into a homogeneous product for energy use in the cement industry. Theprocess reduces the volume of waste for final disposal and extends their life cycle,

allowing their return to productive sector. In countries like Brazil this practice isbecoming very popular.


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9. Conclusion

The objective of the coursework was accomplished, once that the wastewaterwas properly treated and the final effluent reached the UK standards required in

legislation. The SuperPro Designer package had a really important role ongenerating the environmental and economic reports, which aided achieving accurateresults. Besides that, the software also has a large amount of data available and afriendly interface simplifying the assembly of the project and its units.

As shown before, the volume of influent reaching the plant was large.Consequently, the size of the unit processes was relatively sizable which leaded tohigh costs associated to assembly and operating of both of the WWTP.

Finally, the project shown itself feasible considering all the parametersanalysed during the design of the plant.

10. References

[1] West Wind Yorkshire Teasroom (2010) Leeds From Industrial Centre to CallCentre I. Available at:http://www.westwindsinyorkshire.co.uk/attachments/LeedsI.pdf(Accessed at 2 November 2013).

[2] Leeds Population (no date). Available at:http://www.leeds.gov.uk/council/Pages/Leeds-population.aspxx (Accessed at 3November 2013).

[3] Downing, T.E, Butterfield, R.E., Edmonds, B., Knox, J.W., Moss, S., Piper, B.S.andWeatherhead, E.K.(and the CCDeW project team) (2003). Climate Change and theDemandfor Water, Research Report, Stockholm Environment Institute Oxford Office, Oxford.Available at: http://cfpm.org/ccdew/Climate_Change_and_Demand_for_Water-2003.pdf (Accessed at 3 November 2013).

[4] Granular Media Filter (no date). Available at:http://www.mcilvainecompany.com/brochures/liqfil%20brochure/liqfil%20charts/gran%20media%20filters.htm (Accessed at 13 November 2013).

[5] Lenntech Water Treatment Solution (no date). Available at:http://www.lenntech.com.pt/biblioteca/lamas/sludge-drying.htm#ixzz2mGZbIZuS(Accessed at 15 November 2013).

[6] BELTRAME, L. T. C. Caracterizao de Efluente Txtil e Proposta de Tratamento(Characterization of Textile Industry Effluent and Treatment Proposal). 2000. 179p.Masters Thesis (Chemical Engineering). Chemical Engineering Pos-GraduatedProgram, Federal University of Rio Grande do Norte, Natal/RN, Brazil. 2000.

[7] PAUL, S. A.; CHAVAN, S. K. and KHAMBE, S. D. (2012) Studies onCharacterization of Textile Industrial Waste Water in Solapur City, InternationalJournal of Chemical Science, 10(2), pp 635-642.
http://www.westwindsinyorkshire.co.uk/attachments/LeedsI.pdfhttp://www.westwindsinyorkshire.co.uk/attachments/LeedsI.pdfhttp://www.westwindsinyorkshire.co.uk/attachments/LeedsI.pdfhttp://www.leeds.gov.uk/council/Pages/Leeds-population.aspxxhttp://cfpm.org/ccdew/Climate_Change_and_Demand_for_Water-2003.pdfhttp://cfpm.org/ccdew/Climate_Change_and_Demand_for_Water-2003.pdfhttp://cfpm.org/ccdew/Climate_Change_and_Demand_for_Water-2003.pdfhttp://www.mcilvainecompany.com/brochures/liqfil%20brochure/liqfil%20charts/gran%20media%20filters.htmhttp://www.mcilvainecompany.com/brochures/liqfil%20brochure/liqfil%20charts/gran%20media%20filters.htmhttp://www.mcilvainecompany.com/brochures/liqfil%20brochure/liqfil%20charts/gran%20media%20filters.htmhttp://www.lenntech.com.pt/biblioteca/lamas/sludge-drying.htm#ixzz2mGZbIZuShttp://www.lenntech.com.pt/biblioteca/lamas/sludge-drying.htm#ixzz2mGZbIZuShttp://www.lenntech.com.pt/biblioteca/lamas/sludge-drying.htm#ixzz2mGZbIZuShttp://www.mcilvainecompany.com/brochures/liqfil%20brochure/liqfil%20charts/gran%20media%20filters.htmhttp://www.mcilvainecompany.com/brochures/liqfil%20brochure/liqfil%20charts/gran%20media%20filters.htmhttp://cfpm.org/ccdew/Climate_Change_and_Demand_for_Water-2003.pdfhttp://cfpm.org/ccdew/Climate_Change_and_Demand_for_Water-2003.pdfhttp://www.leeds.gov.uk/council/Pages/Leeds-population.aspxxhttp://www.westwindsinyorkshire.co.uk/attachments/LeedsI.pdf


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[8] NOSHEE, S.;NAWAZ, H. and KHALIL-UR-REHMAN. (2000). Physico-ChemicalCharacterization of Effluents of Local Textile Industries of FaisalabadPakistan,International Journal of Agriculture & Biology, Vol. 2, No 3, pp 232-233.

[9] Khan, M. S., Knapp, J., Clemett, A., and Chadwick, M. (2006). "Improving Effluent

Treatment and Management." Report, Key Document, R8161 - Section7, Researchfor Development, Department for International Development (DFID), UK.

[10] Imtiazuddin, S.M.; Mumtaz, M. and Mallick, K. A. (2012). Pollutants ofWastewater Characteristics in Textile Industries, Journal of Basic and AppliedScience, 8, pp 554-556.

[11] Environmental and Heritage Service. (2001). Regulation of Water ServiceDischarge. Available at:http://www.doeni.gov.uk/niea/reg_wsd.pdf(Accessed at 22November 2013).

[12] Council (91/271/EEC) 30 of May 1991, Council Directive concerning urbanwastewater treatment [1991]. No L 135/40.
http://www.doeni.gov.uk/niea/reg_wsd.pdfhttp://www.doeni.gov.uk/niea/reg_wsd.pdfhttp://www.doeni.gov.uk/niea/reg_wsd.pdfhttp://www.doeni.gov.uk/niea/reg_wsd.pdf


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Appendix A Units Mass Balances and Streams Composition

1. Domestic Wastewater Treatment Plant

Clarification P-6

Input Output

ComponentFlowrates (kg/h)

Input S-101 S-102 S-106

A_VSS biomass 28.438 25.594 0.000 2.844

Ammonia 7.719 7.719 0.000 0.000

Carb. Dioxide 12.188 12.188 0.000 0.000

dsticwaste 101.563 100.875 0.000 0.688

I_VSS biomass 14.219 12.797 0.000 1.422

N_VSS biomass 2.519 2.267 0.000 0.252

Nitrogen 0.000 0.000 0.000 0.000

NO2_NO3 1.016 1.009 0.000 0.007

NonBio SS 31.688 9.506 0.000 22.181

NonBio TDS 101.563 100.875 0.000 0.688

Oxygen 0.000 0.000 0.000 0.000

Water 388103.732 385476.077 0.000 2627.655

TOTAL (kg/h) 388404.641 385748.905 0.000 2655.736

TOTAL (L/h) 408316.213 405646.338 0.000 2669.875

Mixing P-4

Input Output


S-101 S-105 Sludge Recycle S-113 S-115

A_VSS biomass 25.594 37.189 278.916 9.582 351.280

Ammonia 7.719 0.000 0.000 0.000 7.719

Carb. Dioxide 12.188 0.000 0.000 0.000 12.188

dsticwaste 100.875 0.000 0.021 0.664 101.560

I_VSS biomass 12.797 0.000 32.294 1.219 46.310

N_VSS biomass 2.267 1.019 7.643 0.280 11.208

Nitrogen 0.000 0.000 0.000 0.000 0.000

NO2_NO3 1.009 0.000 1.317 0.426 2.752

NonBio SS 9.506 5.280 39.601 3.538 57.925

NonBio TDS 100.875 0.000 9.172 3.579 113.625

Oxygen 0.000 0.000 0.000 0.000 0.000

Water 385476.077 217.440 35286.575 16068.015 437048.106

TOTAL (kg/h) 385748.905 260.928 35655.538 16087.302 437752.673

TOTAL (L/h) 405646.338 262.317 35845.364 16172.949 457926.967


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Flow Splitting P-10

Input Output


S-115 S-125 S-126

A_VSS biomass 351.280 175.640 175.640

Ammonia 7.719 3.859 3.859

Carb. Dioxide 12.188 6.094 6.094

dsticwaste 101.560 50.780 50.780

I_VSS biomass 46.310 23.155 23.155

N_VSS biomass 11.208 5.604 5.604

Nitrogen 0.000 0.000 0.000

NO2_NO3 2.752 1.376 1.376

NonBio SS 57.925 28.963 28.963

NonBio TDS 113.625 56.813 56.813

Oxygen 0.000 0.000 0.000

Water 437048.106 218524.053 218524.053

TOTAL (kg/h) 437752.673 218876.336 218876.336

TOTAL (L/h) 457926.967 228963.484 228963.484

Aerobic BioOxidation P-1

Input Output


S-125 S-119 S-128 S-124

A_VSS biomass 175.640 0.000 199.448 0.000

Ammonia 3.859 0.000 0.000 0.000Carb. Dioxide 6.094 0.000 41.489 0.000

dsticwaste 50.780 0.000 0.102 0.000

I_VSS biomass 23.155 0.000 23.817 0.000

N_VSS biomass 5.604 0.000 5.205 0.000

Nitrogen 0.000 76.712 1.117 75.592

NO2_NO3 1.376 0.000 1.472 0.000

NonBio SS 28.963 0.000 29.293 0.000

NonBio TDS 56.813 0.000 56.810 0.000

Oxygen 0.000 23.288 0.000 0.000

Water 218524.053 0.000 218541.993 0.000

TOTAL (kg/h) 218876.336 100.000 218900.745 75.592

TOTAL (L/h) 228963.484 84801.702 244062.539 66018.017


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Input Output


S-126 S-108 S-104 S-127

A_VSS biomass 175.640 0.000 0.000 199.448

Ammonia 3.859 0.000 0.000 0.000

Carb. Dioxide 6.094 0.000 0.000 41.489

dsticwaste 50.780 0.000 0.000 0.102

I_VSS biomass 23.155 0.000 0.000 23.817

N_VSS biomass 5.604 0.000 0.000 5.205

Nitrogen 0.000 76.712 75.592 1.117

NO2_NO3 1.376 0.000 0.000 1.472

NonBio SS 28.963 0.000 0.000 29.293

NonBio TDS 56.813 0.000 0.000 56.810

Oxygen 0.000 23.288 0.000 0.000

Water 218524.053 0.000 0.000 218541.993

TOTAL (kg/h) 218876.336 100.000 75.592 218900.745

TOTAL (L/h) 228963.484 84801.702 66018.017 244062.539

Mixing P-11

Input Output


S-127 S-128 S-103

A_VSS biomass 199.448 199.448 398.895

Ammonia 0.000 0.000 0.000Carb. Dioxide 41.489 41.489 82.979

dsticwaste 0.102 0.102 0.205

I_VSS biomass 23.817 23.817 47.634

N_VSS biomass 5.205 5.205 10.410

Nitrogen 1.117 1.117 2.233

NO2_NO3 1.472 1.472 2.943

NonBio SS 29.293 29.293 58.586

NonBio TDS 56.810 56.810 113.620

Oxygen 0.000 0.000 0.000

Water 218541.993 218541.993 437083.985

TOTAL (kg/h) 218900.745 218900.745 437801.490

TOTAL (L/h) 244062.539 244062.539 488125.078


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Clarification P-3

Input Output


S-103S-

110S-112 Sludge

A_VSS biomass 398.895 0.000 41.321 371.888Ammonia 0.000 0.000 0.000 0.000

Carb. Dioxide 82.979 0.000 99.508 0.000

dsticwaste 0.205 0.000 0.237 0.029

I_VSS biomass 47.634 0.000 4.784 43.059

N_VSS biomass 10.410 0.000 1.132 10.190

Nitrogen 2.233 0.000 2.233 0.000

NO2_NO3 2.943 0.000 14.555 1.756

NonBio SS 58.586 0.000 5.867 52.801

NonBio TDS 113.620 0.000 101.374 12.229

Oxygen 0.000 0.000 0.000 0.000

Water 437083.985 0.000 390019.572 47048.766

TOTAL (kg/h) 437801.490 0.000 390290.582 47540.718

TOTAL (L/h) 488125.078 0.000 449532.655 47793.818

GM Filtration

Input Output


S-112 S-116 S-105 Output


Carb. Dioxide 99.508 0.000 0.000 99.508

dsticwaste 0.237 0.000 0.000 0.237

I_VSS biomass 4.784 0.000 0.000 4.784

N_VSS biomass 1.132 0.000 1.019 0.113

Nitrogen 2.233 0.000 0.000 2.233

NO2_NO3 14.555 0.000 0.000 14.555

NonBio SS 5.867 0.000 5.280 0.587

NonBio TDS 101.374 0.000 0.000 101.374

Oxygen 0.000 0.000 0.000 0.000

Water 390019.572 217.440 217.440 390019.572

TOTAL (kg/h) 390290.582 217.440 260.928 390247.094

TOTAL (L/h) 449532.655 218.597 262.317 449488.936


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Flow Splitting P-5

Input Output


SludgeSludgeRecycle

S-114

A_VSS biomass 371.888 278.916 92.972Ammonia 0.000 0.000 0.000

Carb. Dioxide 0.000 0.000 0.000

dsticwaste 0.029 0.021 0.007

I_VSS biomass 43.059 32.294 10.765

N_VSS biomass 10.190 7.643 2.548

Nitrogen 0.000 0.000 0.000

NO2_NO3 1.756 1.317 0.439

NonBio SS 52.801 39.601 13.200

NonBio TDS 12.229 9.172 3.057

Oxygen 0.000 0.000 0.000

Water 47048.766 35286.575 11762.192

TOTAL (kg/h) 47540.718 35655.538 11885.179

TOTAL (L/h) 47793.818 35845.364 11948.455

Mixing P-12

Input Output


S-114 S-106Sludge Treatment

Line

A_VSS biomass 92.972 2.844 95.816Ammonia 0.000 0.000 0.000

Carb. Dioxide 0.000 0.000 0.000

dsticwaste 0.007 0.688 0.695

I_VSS biomass 10.765 1.422 12.187

N_VSS biomass 2.548 0.252 2.799

Nitrogen 0.000 0.000 0.000

NO2_NO3 0.439 0.007 0.446

NonBio SS 13.200 22.181 35.381

NonBio TDS 3.057 0.688 3.745

Oxygen 0.000 0.000 0.000

Water 11762.192 2627.655 14389.847

TOTAL (kg/h) 11885.179 2655.736 14540.916

TOTAL (L/h) 11948.455 2669.875 14618.330


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Belt Filtration

Input Output


Sludge TreatmentLine

S-111 S-113 S-120


Carb. Dioxide 0.000 0.000 0.000 0.000

dsticwaste 0.695 0.000 0.664 0.031

I_VSS biomass 12.187 0.000 1.219 10.968

N_VSS biomass 2.799 0.000 0.280 2.519

Nitrogen 0.000 0.000 0.000 0.000

NO2_NO3 0.446 0.000 0.426 0.020

NonBio SS 35.381 0.000 3.538 31.843

NonBio TDS 3.745 0.000 3.579 0.166

Oxygen 0.000 0.000 0.000 0.000

Water 14389.847 2423.486 16068.015 745.318

TOTAL (kg/h) 14540.916 2423.486 16087.302 877.100

TOTAL (L/h) 14618.330 2436.388 16172.949 881.769

Sludge Drying

Input Output


S-120 S-121 S-122 Dried Sludge


Carb. Dioxide 0.000 0.000 0.000 0.000

dsticwaste 0.031 0.000 0.000 0.031

I_VSS biomass 10.968 0.000 7.714 3.254

N_VSS biomass 2.519 0.000 0.000 2.519

Nitrogen 0.000 3643.249 3643.249 0.000

NO2_NO3 0.020 0.000 0.000 0.020

NonBio SS 31.843 0.000 0.000 31.843

NonBio TDS 0.166 0.000 0.000 0.166

Oxygen 0.000 1106.020 1106.020 0.000

Water 745.318 0.000 524.204 221.114

TOTAL (kg/h) 877.100 4749.269 5281.187 345.182

TOTAL (L/h) 881.769 4027461.098 6183622.038 351.528


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2. Industrial Wastewater Treatment Plant

Mixing P-9

Input Output


Input S-105Sludge

RecyclingS-117 S-102

A_VSS biomass 0.000 9.770 293.094 39.079 341.943

Ammonia 0.404 0.000 0.000 0.000 0.404

Carb. Dioxide 128.855 0.000 0.000 0.000 128.855

Glucose 276.216 0.000 0.000 0.000 276.216

Heavy Metals 4.424 0.517 13.650 3.520 22.111

I_VSS biomass 0.000 0.106 3.180 25.259 28.544

Nitrogen 0.000 0.000 0.000 0.000 0.000

NO2_NO3 0.822 0.030 0.093 0.000 0.945

NonBio SS 0.000 0.197 5.915 0.789 6.901

Oxygen 0.000 0.000 0.000 0.000 0.000

Phenol 0.098 0.003 0.009 0.000 0.109

Water 270219.100 11415.034 10258.816 271656.578 312753.811

TOTAL (kg/h) 270629.920 11425.656 31092.387 411.877 313559.840

TOTAL (L/h) 344106.222 11486.027 31245.842 410.956 387249.047


Input Output


S-102 S-113 S-103 S-104

A_VSS biomass 341.943 0.000 0.000 424.512

Ammonia 0.404 0.000 0.000 1.613

Carb. Dioxide 128.855 0.000 196.058 21.784

Glucose 276.216 0.000 0.000 38.137

Heavy Metals 22.111 0.000 0.000 22.111

I_VSS biomass 28.544 0.000 0.000 30.962

Nitrogen 0.000 76.712 0.000 76.712

NO2_NO3 0.945 0.000 0.000 0.945NonBio SS 6.901 0.000 0.000 8.110

Oxygen 0.000 23.288 0.000 9.385

Phenol 0.109 0.000 0.000 0.001

Water 312753.811 0.000 0.000 312829.510

TOTAL (kg/h) 313559.840 100.000 196.058 313463.782

TOTAL (L/h) 387249.047 84801.702 108988.809 403596.310


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Input Output


S-104 S-120 S-108 S-106

A_VSS biomass 424.512 0.000 0.000 435.692

Ammonia 1.613 0.000 0.000 2.178

Carb. Dioxide 21.784 0.000 38.527 4.281

Glucose 38.137 0.000 0.000 0.000

Heavy Metals 22.111 0.000 0.000 22.111

I_VSS biomass 30.962 0.000 0.000 32.091

Nitrogen 76.712 76.712 0.000 153.421

NO2_NO3 0.945 0.000 0.000 0.945

NonBio SS 8.110 0.000 0.000 8.674

Oxygen 9.385 23.288 0.000 26.181Phenol 0.001 0.000 0.000 0.088

Water 312829.510 0.000 0.000 312839.594

TOTAL (kg/h) 313463.782 100.000 38.527 313525.255

TOTAL (L/h) 403596.310 84801.702 21417.236 474503.842

Clarification

Input Output

Component

Flowrates (kg/h)

S-106S-

107S-121 Sludge

A_VSS biomass 435.692 0.000 43.421 390.792

Ammonia 2.178 0.000 2.172 0.000

Carb. Dioxide 4.281 0.000 4.285 0.000

Glucose 0.000 0.000 0.000 0.000

Heavy Metals 22.111 0.000 3.911 18.200

I_VSS biomass 32.091 0.000 28.065 4.239

Nitrogen 153.421 0.000 153.421 0.000

NO2_NO3 0.945 0.000 0.821 0.124

NonBio SS 8.674 0.000 0.876 7.887

Oxygen 26.181 0.000 26.252 0.000Phenol 0.088 0.000 0.077 0.012

Water 312839.594 0.000 271656.578 41035.262

TOTAL (kg/h) 313525.255 0.000 271919.879 41456.516

TOTAL (L/h) 474503.842 0.000 432740.944 41661.123


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GM Filtration

Input Output


S-121 S-119 S-117 Output

A_VSS biomass 43.421 0.000 39.079 4.342

Ammonia 2.172 0.000 0.000 2.172

Carb. Dioxide 4.285 0.000 0.000 4.285

Glucose 0.000 0.000 0.000 0.000

Heavy Metals 3.911 0.000 3.520 0.391

I_VSS biomass 28.065 0.000 25.259 2.807

Nitrogen 153.421 0.000 0.000 153.421

NO2_NO3 0.821 0.000 0.000 0.821

NonBio SS 0.876 0.000 0.789 0.088

Oxygen 26.252 0.000 0.000 26.252Phenol 0.077 0.000 0.000 0.077

Water 271656.578 343.231 271656.578 30776.447

TOTAL (kg/h) 271919.879 343.231 411.877 271851.233

TOTAL (L/h) 432740.944 345.058 410.956 432675.046

Flow Splitting P-9

Input Output

Component

Flowrates (kg/h)

SludgeSludge

RecyclingSludge Treatment

Line

A_VSS biomass 390.792 293.094 97.698

Ammonia 0.000 0.000 0.000

Carb. Dioxide 0.000 0.000 0.000

Glucose 0.000 0.000 0.000

Heavy Metals 18.200 13.650 4.550

I_VSS biomass 4.239 3.180 1.060

Nitrogen 0.000 0.000 0.000

NO2_NO3 0.124 0.093 0.031

NonBio SS 7.887 5.915 1.972

Oxygen 0.000 0.000 0.000Phenol 0.012 0.009 0.003

Water 41035.262 10258.816 0.000

TOTAL (kg/h) 41456.516 31092.387 10364.129

TOTAL (L/h) 41661.123 31245.842 10415.281


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Belt Filtration

Input Output


SludgeTreatment Line

S-112 S-111 S-105

A_VSS biomass 97.698 0.000 87.928 9.770

Ammonia 0.000 0.000 0.000 0.000

Carb. Dioxide 0.000 0.000 0.000 0.000

Glucose 0.000 0.000 0.000 0.000

Heavy Metals 4.550 0.000 4.033 0.517

I_VSS biomass 1.060 0.000 0.954 0.106

Nitrogen 0.000 0.000 0.000 0.000

NO2_NO3 0.031 0.000 0.001 0.030

NonBio SS 1.972 0.000 1.774 0.197

Oxygen 0.000 0.000 0.000 0.000Phenol 0.003 0.000 0.000 0.003

Water 0.000 1669.934 513.716 11415.034

TOTAL (kg/h) 10364.129 1669.934 608.406 11425.656

TOTAL (L/h) 10415.281 1678.824 608.078 11486.027

Sludge Drying

Input Output

Component

Flowrates (kg/h)

S-111 S-114 S-116Dried

Sludge

A_VSS biomass 87.928 0.000 0.000 87.928

Ammonia 0.000 0.000 0.000 0.000

Carb. Dioxide 0.000 0.000 0.000 0.000

Glucose 0.000 0.000 0.000 0.000

Heavy Metals 4.033 0.000 0.000 4.033

I_VSS biomass 0.954 0.000 0.000 0.954

Nitrogen 0.000 2314.102 2314.102 0.000

NO2_NO3 0.001 0.000 0.000 0.001

NonBio SS 1.774 0.000 0.000 1.774

Oxygen 0.000 702.517 702.517 0.000Phenol 0.000 0.000 0.000 0.000

Water 513.716 0.000 337.861 175.854

TOTAL (kg/h) 608.406 3016.619 3354.480 270.545

TOTAL (L/h) 608.078 2558144.012 3927684.292 271.900


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Appendix B Meetings Minutes

21/10: First group meeting, when we made the Project Plan in order to organize thetasks and next meetings. It was noticed the need of a population projection and thecomposition of the industrial wastewater. Everyone agreed to do some study on the

scope of the project until the next meeting.

28/10: The members of the group decided to do some research about the populationprojection in favour of choosing a good method for the estimates to be appropriate.In addition, the characteristics of the industrial wastewater required attention oncethat it is crucial for precise treatment. Another meeting was scheduled for 07/11. Theproject plan can be seen below:

07/11: The population projection was defined and calculated which also helped withthe definition of the design of the plant. The members of the group are supposed todo some research for the next days in order to find out the best way of treatment and

spend some time using SuperPro software to improve their abilities on it.

12/11: Meeting arranged for discussion about design of the Wastewater TreatmentPlant considering the wastewater composition. All the members had a discussionabout the domestic plant and started the design of it.

14/11: The group worked on the design of the domestic WWT plant, considering allthe information collected before.

18/11: Start of the design on the industrial WWT plant.

22/11: The design of both plants was finished, and the flow sheets were properlyorganized to facilitate viewing.

23/11: The group began to write the report, explaining all the calculations andinformation used on it.

27/11: Meeting arranged for final adjustments in the report, formatting and revisions.

28/11: The group started to prepare the presentation, discussing the main issues tobe addressed and the best way to do it, in order to meet the time set by the lecturer.

30/11: The presentation was finished and final revision was made to correct possible

Final Coursework

Documents

Transcript of Final Coursework