Textile Effluent Treatment Process

7/29/2019 Textile Effluent Treatment Process

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European Journal of Scientific Research

ISSN 1450-216X Vol.53 No.1 (2011), pp.6-16 EuroJournals Publishing, Inc. 2011

http://www.eurojournals.com/ejsr.htm

Textile Effluent Treatment with Reverse Osmosis

Membrane using Anova Model

M. Ramesh Kumar

Department of Textile Technology, SSM College of Engineering, Komarapalayam

Namakkal, Tamilnadu, India - 638 183

E-mail: [email protected]

Tel: + 91 098 9431 0132; Fax: + 04288 267702

K. Saravanan

Department of Chemical Engineering, Kongu Engineering College, Perundurai

Erode, Tamilnadu, India - -638 052

E-mail: [email protected]: + 91 098 4270 5656

Abstract

Textile dyeing industry involves a variety of chemicals comprising various classesof dyes and pigments along with a huge amount of water which is required for this

operation. This industry consumes a vast quantity of water and generates an equally vast

quantity of wastewater. This paper is concerned with the wastewater characteristics of

textile knitted fabric dyeing industry. The membrane selection process was theoreticallydesigned using well known design softwares like KOCH and ROSA. To design treatment

plant system based on the analytical report and software membrane Reverse Osmosis (RO)

system. To compare experimental and theoretical (KOCH and ROSA Software) values forthe characteristics of dyeing industry. The results reveal that the Koch software membrane

produces better results to treat the effluent from the knitted fabric effluent. The results were

comparison of analysis of variances (Anova) methods.

Keywords: Anova method, algorithms, knitted fabric dyeing, KOCH and ROSA software

membrane, Reverse Osmosis, textile effluent, treatment.

1. IntroductionDrewes (2003) study the Reverse osmosis (RO) membranes are widely used in drinking water,

wastewater and industrial applications. The use of RO membranes in advanced wastewater reclamation

using secondary treated wastewater effluent to produce water for indirect potable use has alsoincreased over the past few years. However, a major impediment in the application of RO membrane

technology for desalination and wastewater reclamation is membrane fouling. Barker (2000)

investigate the advanced water reclamation, secondary effluent from wastewater treatment plants

contains dissolved organic matter, commonly known as effluent organic matter. When the secondwastewater effluent is introduced to the RO membrane processes as feed water, the presence of effluent

organic matter contributes to organic fouling.


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Textile Effluent Treatment with Reverse Osmosis Membrane using Anova Model 7

Amjad (1993) study the membrane based separation processes like Ultrafiltration (UF) and

Reverse Osmosis (RO) have been applied for treating a wide variety of industrial effluents.

Chain (1977) investigate the most of the effluents from different industrial source were used tobe discharged directly in the soil or in ground water. But due to stringent environmental restrictions,

Central Pollution Control Board (CPCB) has become vigilant and has imposed very stringent measures

for recovering pure water from such industrial effluents. However, for the treatment of an effluent by

conventional methods like aerobic and non-aerobic digestion, the ratio of biological oxygen demand

(BOD) to COD should be >0.6.Walter (2006) study the membrane processes, namely, reverse osmosis (RO), nanofiltration

(NO), ultrafitration (UF) and microfiltration (MF) are continuing to get more and more attention worldwide for their effectiveness in water treatment. RO got recognition as an alternative option among

other conventional treatment processes in the early 1960s when it was successfully used for the first

time in the desalination of seawater. As a result of continuous research and development in this field, anew generation of RO membranes which can operate under ultra-low pressure was developed in the

beginning of 1995. This new generation of RO and NF were able to produce double the quantity of

flux of the conventional RO and NF at low operating pressure without sacrificing the quality of theproduced water by keeping the rejection of the organic and inorganic species at the same level.

Schwinge (2004) study the membranes are manufactured in different shapes and configurations,

the most popular are spiral wound membrane (SWM), hollow fibre, tubular and frame and platemodule with the target to reach an optimal performance for both operating conditions andconfigurating modules. Studying how different variables in the process change along the membrane

play an important role in the optimization process and it was the issue for most of the researches both

numerically and experimentally. Previous studies reported that across the longitudinal direction of theSWMs a fall in the permeate flow rate and a rise in the permeate and concentrate concentrations always

took place.

Brian (1965) study the finite difference method was used by Brian to calculate the saltconcentration polarization over the length of the membrane for the case of permeate surface. The

results obtained were compared with a constant flux model across the membrane length.

Bhattacharyya (1990) investigate in used a finite element method to predict flux behaviour and

concentration polarization throughout various configurations of RO membranes. The results obtainedfrom this study were in total agreement with previous work regarding increase in concentration and

decrease in permeate flux along the membrane length.

Fletcher (2004) In another numerical study, the effect of gravity on the permeation velocity andsalt mass fraction through out the membrane were investigated. Their results showed that the effect of

gravity cannot be overlooked along the channel with the adverse gravity conditions giving the highest

salt concentrations and lowest flux at the membrane surface.Drewes (2006) investigate the RO process is gaining wider use for contaminant removal in

advanced water and wastewater treatment and desalination. Advancements in membrane developments

result in the production of better and more economical membranes. These are yielding the desired

result of being adopted as an efficient water treatment technology. However, membrane fouling is still

a great hindrance for operation and cost efficiency. Fouling phenomena could severely limit membraneprocess efficiency as they lead to several deleterious effects including flux decline, possible permeate

quality decrease and a gradual membrane degradation. An uneconomical increase in applied pressureand the need for frequent cleaning (shortening membrane life) or replacement become the necessary

options if the rate of water production is to be maintained constant. The effect of fouling has been

investigated extensively by numerous researchers.Machenbach (1998) study the membrane process the increasing cost of water and its wasteful

consumption have now induced a treatment process which is integrated in in-plant water circuits rather

than as a subsequent treatment. From this standpoint, membrane filtration offers potential applications.Processes using membranes provide very interesting possibilities of separating hydrolyzed dyestuffs

and dyeing auxiliaries, thus simultaneously reducing coloration and the BOD/COD of the wastewater.


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8 M. Ramesh Kumar and K. Saravanan

Tinghui (1983) investigate the Reverse osmosis membranes have a retention rate of 90% or

more for most types of ionic compounds and produce a high quality of permeate. Decoloration and the

elimination of chemical auxiliaries in dye house wastewater can be carried out in a single step. Reverseosmosis permeates the removal of all mineral salts, hydrolyzed reactive dyes and chemical auxiliaries.

The problem involved is that the higher the concentration of salts, the more important the osmotic

pressure becomes and therefore the greater the energy required.

Erswell (1988) study the Nanofiltation membranes retain organic compounds of low molecular

weight, divalent ions or large monovalent ions, such as hydrolyzed reactive dyes as well as dyeingauxiliaries. (Tang, 2002) investigate the effect of the concentration of dyes has been frequently

reported in dye house effluents as well as the concentration of salt and the pressure. In most publishedstudies concerning dye house effluents, the concentration of mineral salts does not exceed 20 g L -1 and

the concentration of dyestuff 1.5 g L-1.

(Abari, 2002) study the effluents are reconstituted with

generally only one dye and the volume studied is low. (Freger, 2000) study the treatment of wastewaterafter dyeing by nanofiltration thus represents one of the rate applications possible for the treatment of

solutions with highly concentrated and complex solution.

Watters (1991) study the Ultrafiltration enables the elimination of macromolecules andparticles but the elimination of polluting substances, such as color is never complete (between 31% and

76%). (Rott, 1999) study the even in the best of cases, the quality of the treated wastewater does not

permit its reuse for feeding sensitive processes, such as the dyeing of textile. Ciardelli (2001) studyUltrafiltration can only be used as a pretreatment for reverse osmosis or in combination with abiological reactor. (Mignani, 1999)

Al-Malack, (1997) study the Microfiltration is suitable for treating dye baths containing

pigment dyes as well as subsequent rinsing baths. Sadr Ghayeni (1998) investigate the auxiliariesremain in the retentant. Microfiltration can be used as a pretreatment for nanofiltration or reverse

osmosis

Hitendra Bhuptawat (2007) investigates the water extract of Moringa. Oleifera seed wasapplied to a treatment sequence comprising coagulation-flocculation-sedimentation-sand filtration.

Model waters (kaolinite suspensions) of turbidities 10, 100, 300 and 700 NTU were prepared. For the

10 NTU water, the optimum dose was only evident when sand filtration was incorporated into the

treatment.Zhi Lin Li, Wei Liu, Xin Fang. Chen (2010) study the feasibility of using laccase to treat oily

wastewater was examined. When only laccase was added to the synthetic oily wastewater, the suitable

technological conditions were laccase at 3 U/ml, pH at 6.0, a temperature of 30C, and a reaction timeof 6 h for the initial oil concentration of 120 mg/L. Under those conditions, the rate of oil removal was

as high as 69%. The effects of Mg2+

, Mn2+

, Cu2+

, and Fe2+

ions in wastewater on the rate of oil removal

using laccase were investigated. The results showed that Cu2+

and Fe2+

ions obviously inhibited thecatalytic performance of laccase under the studied concentration. On the other hand, Mg2+ and Mn2+

ions only had slight effects on the rate of oil removal for the range of concentrations studied. A 95% oil

removal rate could be obtained when actual wastewaters were treated using laccase with the additive

chitosan under the suitable technological conditions.

Fons Moi. Pang, Sheau Ping. Teng, Tjoon Tow. Teng (2009) investigates the hydroxideprecipitation and coagulation-flocculation methods were used to treat wastewater containing lead, zinc,

copper, and iron. The concentrations of heavy metals in the synthetic wastewater range from 1 to 14mg/L for lead, 5 to 90 mg/L for zinc, 3 to 90 mg/L for copper and 5 to 45 mg/L for iron. Individual

Zn(II) and Cu(II) with concentrations below 90 mg/L and Fe(III) with concentrations below 45 mg/L

were removed up to 99% by the precipitation method in the pH range of 8.7 to 9.6, 8.1 to 11.1, and 6.2to 7.1, respectively.

Daniel Babineau, Dominique Chartray, Roland Leduc (2009) investigates the treatment of

municipal wastewaters by physical-chemical methods normally requires the use of a metallic saltcoagulant and a synthetic coagulant aid. Integrating the sustainable development concept in the


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treatment of waters favours the use of renewable resources such as natural biopolymers. In order to

better understand the peculiarities of using a product of natural origin in municipal wastewater

treatment, laboratory testing (jar tests) was achieved with chitosan as a coagulant aid, as well as full-scale testing in a medium size physical-chemical wastewater treatment plant. The full-scale test was

performed in two parallel, identical systems treating the same wastewater under the same conditions.

The one using a combination of alum with a synthetic polymer (AL/SP) was compared with the other

which used alum and chitosan (AL/CH). Removals for COD, SS, and total phosphorus reached 87%,

95% and 93%, respectively, for the AL/CH combination. These results are similar to those obtained forCOD and SS with the AL/SP combination. Some results show a coagulant dosage (alum) up to 24.8%

lower with chitosan as the usual coagulant aid. For total phosphorus, however, the results show thatremovals were higher with the AL/SP combination because of a higher coagulant dosage.

2. Research MethodThis work carried out Sakthi Knitting private Limited., located at SIPCOT, Perundurai, Erode, Tamil

Nadu, India. Manufacturing in Knitting fabric dyeing including eight numbers of soft flow reactorsdyeing machine (batch process), five numbers of Winch dyeing machine are used for knitted fabric

dyeing with different capacities, including scouring, bleaching, mercerization and dyeing. The total

quantity of fabric processed in knitted fabric dyeing 1500 2000 kgs/day and the volume of effluentgenerated is of the order of 500 600 m/day.

Effluent samples were collected and tested as per American Public Health Association

(APHA) in knitted fabric dyeing industry for following parameters such as pH, TDS, BOD, COD,Cl , Ca2+, Mg2+, Na+, K+, NH4+, HCO3 , SO4

2-, NO3 and SiO2. Collection of datas 3 times per day

that is 9.00 am, 1.00 pm and 5.00 pm continuously 14 days.

Table 1: Knitted fabric dyeing collection of datas for input parameters

Knitted Fabric Dyeing

ParametersTime 9.00 am X1 Time 1.00 pm X2 Time 5.00 pm X3

pH 7.40 7.66 7.52TDS 4120 4066 4108

COD 50 44 46

BOD 3 2 3

Cl-

2040 1998 2022

Ca+

37 34 32

Mg+

16 914 15

Na+

1552 1519 1487

K+

4 5 5

NH4+

0.72 0.86 0.77

HCO3 340 362 371

SO42

271 286 292

NO3-

0.76 086 0.86

SiO2 16 18 19

Table 1 shows the datas collected X1, X2, X3 three timesper day from knitted fabric dyeing

effluent parameters.

2.1. Using KOCH Software

In KOCH software membrane is ROPRO RO stage-I, used TFC 8040 XR 375 and RO stage-II, TFC

8040 SW 335 membranes. In Array classification RO stage-I, 5X6:3X6 and RO stage-II, 2X5:1X5.Number of elements used in RO stage-I, 48, stage-II, 15 and total 63 elements.

RO feed flow 30.0 m3/hr, permeate flow 27.0 m3/hr, reject flow 3.0 m3/hr and RO recovery

90.00%. Pressure required in RO stage-1, 11.6 kgs/cm2, stage-II, 14.7 kgs/cm

2.


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Table 2: Koch Software membrane data

S.No Parameters KOCH Software

01. Membrane: ROPRO

RO Stage I TFC 8040 XR 375

RO Stage II TFC 8040 SW 335

Table 2, shows the Koch software membrane for Reverse Osmosis (RO) stage I and II.Where, TFC = Thin Flim Composite membrane

XR = Extra Rejection

SW = Sea Water

375 = Membrane Active Area 375 feet square335 = Membrane Active Area 335 feet square

Table 3: RO feed and KOCH software permeate parameters value for knitted fabric dyeing

S.No ParametersRO Feed

(In put)

Theoretical value for RO

Permeate KOCH Software

(Out put)

01 pH 7.70 4.9202 TDS 4039.92 93.62

03 COD 45 ---

04 BOD 2 ---

05 Cl 2010 51.31

06 Ca 35 0.15

07 Mg 15 0.06

08 Na 1500 36.22

09 K 5.0 0.16

10 NH4 0.70 0.05

11 HCO3 350 8.12

12 SO4 280 1.03

13 NO3 0.80 0.09

14 SiO2

17.00 0.40

Table 3, shows the Reverse Osmosis feed and KOCH software membrane permeate parameters.

2.2. Using ROSA Software

In ROSA software membrane is FILMTEC RO stage-I, used BW 30 365 FR and RO stage-II, SW

30 HR - 380 membranes. In Array classification RO stage-I, 5X6:3X6 and RO stage-II, 2X5:1X5.

Number of elements used in RO stage-I, 48, stage-II, 15 and total 63 elements.RO feed flow 30.0 m3/hr, permeate flow 27.10 m3/hr, reject flow 2.99 m3/hr and RO recovery

90.03%. Pressure required in RO stage-1, 11.20 kgs/cm2, stage-II, 14.30 kgs/cm2.

Table 4: Rosa Software membrane data

S.No Parameters ROSA Software

01. Membrane: FILMTEC

RO Stage I BW 30 365 FR

RO Stage II SW 30 HR 380

Table 4, shows the Rosa software membrane for Reverse Osmosis (RO) stage I and II.

Where, SW = Sea WaterBW = Brackish Water

FR = Fine Rejection


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HR = High Rejection

365 = Membrane Active Area 365 feet square

380 = Membrane Active Area 380 feet square

Table 5: RO feed and ROSA software permeate parameters value for knitted fabric dyeing

S.No Parameters

RO Feed

(In put)

Theoretical value for RO

Permeate KOCH Software(Out put)

01 pH 7.70 5.28

02 TDS 4039.92 324.47

03 COD 45 ---

04 BOD 2 ---

05 Cl 2010 172.12

06 Ca 35 0.87

07 Mg 15 0.38

08 Na 1500 121.10

09 K 5.0 0.45

10 NH4 0.70 0.22

11 HCO3 350 17.40

12 SO4 280 10.30

13 NO3 0.80 0.59

14 SiO2 17.00 0.90

Table 5, shows the Reverse Osmosis feed and ROSA software membrane permeate parameters.

2.3. Using Experimental Method

Koch and Rosa software membrane used RO feed parameters same values use in Experimental ROfeed.

Table 6: RO feed and Experimental permeate value of RO for knitted fabric dyeing

S.No Parameters RO Feed

(In put)

Experimentalvalue for RO

Permeate

(Out put)

01 pH 7.70 5.44

02 TDS 4039.92 202.32

03 COD 45 1.71

04 BOD 2 ---

05 Cl 2010 81.00

06 Ca 35 0.36

07 Mg 15 0.11

08 Na 1500 61.36

09 K 5.0 0.21

10 NH4 0.70 0.07

11 HCO3 350 11.1612 SO4 280 2.96

13 NO3 0.80 0.13

14 SiO2 17.00 0.69

Table 6, shows the RO feed and experimental permeate value for knitted fabric dyeing


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2.4. Flow Chart

Figure 1: Flow chart of knitted fabric dyeing effluent treatment

Knitted Fabric Effluent

Collection data

Using KOCH

Software

Membrane

Using

ANOVA

Method

Using ROSA

software

Membrane

Yes YesNo

Low /

Accepted

Low /

Accepted

High / Not

Accepted

2.5. Algorithm

STEP -1: Data processingSTEP 2: Using Anova method

STEP 3: To find TSS,

TSS =N

Txxx

223

22

21 ++

STEP - 4: To find SSC,

SSC =N

T

N

x

N

x

N

x 2

1

2

3

1

2

2

1

2

1 )()()(++

STEP 5: To find SSR,

SSR = N

T

N

y

N

y

N

y

N

y 2

2

2

14

2

2

3

2

2

2

2

2

1 )(

.....

)()()(

++++

STEP 6: To find SSE,

SSE = TSS SSC SSR

STEP 7: Using Anova table

STEP -8: Results:


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Table 7: Analysis of variance design of experimental for rejection measurement for knitted fabric dyeing

effluent

Factor Sum of squares Degree of Freedom Means Square Variance F Ratio

Between Column 49.00 2 24.5 - 0.082 3.32

Between Rows 8407.98 13 646.76 - 2.169 2.01

Residual - 7751 26 - 298.11 --- ---

Total 705.98 41 376.15 --- ---

There is difference between Koch, Rosa softwares and Anova values.

3. Results and DiscussionsThe total quantity of fabric processed in knitted fabric dyeing unit is 1500 2000 kgs/day and the

volume of effluent generated is of the order of 500 600 m/day.

Table 8: Comparison in RO feed, permeate reduction % of Experimental value and Theoretical value in

Knitted fabric dyeing 600 KLD capacity

S.No ParametersAverage

RO Feed

Experimental data for ROPermeate

Theoretical data for RO PermeateKOCH Software ROSA Software

RO

Permeate

RO

Reduction %

RO

Permeate

RO

Reduction

%

RO

Permeate

RO

Reduction

%

01 pH 7.70 5.44 29.35% 4.92 36.10% 5.28 31.42%

02 TDS 4039.92 202.32 94.99% 93.62 97.68% 324.47 91.96%

03 COD 45 1.71 96.20% --- --- --- ---

04 BOD 2 --- --- --- --- --- ---

05 Cl 2010 81.00 95.97% 51.31 97.47% 172.12 91.43%

06 Ca2+

35 0.36 98.97% 0.15 99.57% 0.87 97.51%

07 Mg2+

15 0.11 99.26% 0.06 99.60% 0.38 97.46%

08 Na+

1500 61.36 95.90% 36.22 97.58% 121.10 91.92%

09 K+

5.0 0.21 95.80% 0.16 96.80% 0.45 91.00%

10 NH4+ 0.70 0.07 90.005 0.05 92.85% 0.22 68.57%11 HCO3 350 11.16 96.82% 8.12 97.68% 17.40 95.02%

12 SO42-

280 2.96 98.945 1.03 99.63% 10.30 96.32%

13 NO3 0.80 0.13 83.75% 0.09 88.75% 0.59 26.25%

14 SiO2 17.00 0.69 95.94% 0.40 97.64% 0.90 94.70%

Table 8 represent the combine values of all the three parameters, that are experimental values ofRO feed, permeate and RO reduction %. Theoretical value of Koch software in RO feed, permeate and

RO reduction %. Theoretical value of Rosa software in RO feed, permeate and RO reduction %.

Table 9: Comparison between Koch and Rosa Software in 600 KLD capacity for Knitted Fabric Dyeing

S.No Parameters KOCH SOFTWARE ROSA SOFTWARE01. Membrane: ROPRO FILMTEC

RO Stage I TFC 8040 XR - 375 BW 30 365 FR

RO Stage II TFC 8040 - SW 335 SW 30 HR 380

02. Array Classification:

RO Stage I 5 X 6: 3 X 6 5 X 6: 3 X 6

RO Stage II 2 X 5: 1 X 5 2 X 5: 1 X 5

03. No. of Elements used:

RO Stage I 48 Elements 48 Elements

RO Stage II 15 Elements 15 Elements

Total 63 Elements 63 Elements

04. No. of working hours in RO 20Hrs 20 Hrs

05. Recovery 90.00% 90.03%


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Table 9: Comparison between Koch and Rosa Software in 600 KLD capacity for Knitted Fabric Dyeing -

continued

06. Feed TDS 4039 ppm 4039 ppm

07. Permeate TDS 93.62 ppm 324.47 ppm

08. TDS Reduction % 97.68 % 91.96 %

09. Average Membrane Flux 9.6 LMH 12.52 LMH

10. Power Consumption in Kw 19.33 KW 32.12 KW

11. Membrane cost Rs. 25,000 to 30,000 Rs. 35,000 to 40,00012. Handling of projection Simple Complicated

13. Investment Cost Less Compare to Koch higher

14 RO Feed Flow 30 m/hr 30.00 m/hr

RO Permeate Flow 27 m/hr 27.10 m/hr

RO Reject Flow 3 m/hr 2.99 m/hr

RO Recovery % 90.00 % 90.03 %

Table 9 show the Koch and Rosa software membranes for knitted fabric dyeing compare the

following parameters like, TDS reduction %, average membrane flux, power consumption, bothmembrane cost, investment cost, RO feed flow, permeate flow, reject flow.

Table 10: Comparison between Koch Software and Experimental Selected Membrane Results for 600 KLD inKnitted Fabric Dyeing

S.No.Parameters KOCH Software Results

Experimental Selected

Membrane Results

01. Membrane: ROPRO ROPRO

RO Stage I TFC 8040 XR - 375 TFC 8040 XR - 375

RO Stage II TFC 8040 - SW 335 TFC 8040 - SW 335

02. Array Classification:

RO Stage I 5 X 6: 3 X 6 5 X 6: 3 X 6

RO Stage II 2 X 5: 1 X 5 2 X 5: 1 X 5

03. No. of Elements used:

RO Stage I 48 Elements 48 Elements

RO Stage II 15 Elements 15 Elements

Total 63 Elements 63 Elements

04. No. of working hours in RO 20Hrs 20 Hrs

05. Recovery 90.00% 90.27%

06. Feed TDS 4039 ppm 4039 ppm

07. Permeate TDS 93.62 ppm 202.32 ppm

08. TDS Reduction % 97.68 % 95.00 %

09. Average Membrane Flux 9.6 LMH 10.1 LMH

10. Power Consumption in KW 19.33 KW 20.26 KW

11 Flow Rate:

RO Feed Flow 30 m/hr 29.80m/hr

RO Permeate Flow 27 m/hr 26.90 m/hr

RO Reject Flow 3 m/hr 2.90 m/hr

RO Recovery % 90.00 % 90.27 %12 Pressure:

RO 1st Stage 11.6 Kgs/cm 11.20 Kgs/cm

RO 2nd

Stage 14.7 Kgs/cm 14.30 Kgs/cm

Table 10 shows the results also reveal that the Koch software membrane is recommended totreat the effluent from the knitted fabric dyeing.


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4. Conclusions In KOCH Software membrane,

o Higher TDS Reductiono Higher RO Recovery %o Power consumption is lesso Investment cost is less as compare to ROSA software membrane.

From the experimental and theoretical results, it can be seen that characteristics of effluent fromRO feed and permeate water, the following range of percentage reduction were observed as,

o TDS 91.96 97.68 %o Cl 91.43 97.47 %o Ca2+ 97.51 99.57%o Mg2+ 97.46 99.26%o SO42- 96.32 98.94%o SiO2 97.40 98.20 %The analysis of variances in knitted fabric effluent using Reverse Osmosis software membrane,

Koch software shows better results as compared to Rosa software. Also the Anova mathematical model

application results has minor variations as compared with the out put results of software membrane.In Koch TDS reduction 97.68% where as in Rosa 91.96 %, In Koch RO Recovery 90.00%

where as in Rosa 90.03%, In Koch power consumption is 19.33 KW where as in Rosa 32.12 KW. Theabove results reveal that the Koch software membrane is recommended to treat the effluent from theknitted fabric dyeing industry. Both software membranes comparatively the Koch software membraneis better results to treat the knitted fabric dyeing effluents. Cost effective method of producing low

salinity recycled water for industrial applications and indirect potable reuse. To successfully use RO

membrane for the treatment of the knitted fabric dyeing effluents.

AcknowledgementThe author would like to thanks M/S Sakthi Knitting private Limited. SIPCOT, Perundurai, Erode,

Tamil Nadu, India.

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solutions, Water Quality Research Journal of Canada, Vol. 44 (2):pp 174 182.[16] Hitendra Bhuptawat, G.K. Folkard, Sanjeev Chaudhari, 2007. Laboratory evaluation of a

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Textile Effluent Treatment Process